JP2021046572A5 - - Google Patents
Download PDFInfo
- Publication number
- JP2021046572A5 JP2021046572A5 JP2019168541A JP2019168541A JP2021046572A5 JP 2021046572 A5 JP2021046572 A5 JP 2021046572A5 JP 2019168541 A JP2019168541 A JP 2019168541A JP 2019168541 A JP2019168541 A JP 2019168541A JP 2021046572 A5 JP2021046572 A5 JP 2021046572A5
- Authority
- JP
- Japan
- Prior art keywords
- nickel oxide
- slurry
- ore slurry
- oxide ore
- ore
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000002002 slurry Substances 0.000 claims description 102
- 229910000480 nickel oxide Inorganic materials 0.000 claims description 50
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 claims description 50
- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 40
- 238000004062 sedimentation Methods 0.000 claims description 28
- 239000002253 acid Substances 0.000 claims description 25
- 229910052759 nickel Inorganic materials 0.000 claims description 20
- 239000007788 liquid Substances 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- 238000000926 separation method Methods 0.000 claims description 8
- 230000001112 coagulant Effects 0.000 claims description 6
- 239000000701 coagulant Substances 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 6
- 238000010979 pH adjustment Methods 0.000 claims description 4
- 238000010306 acid treatment Methods 0.000 claims description 3
- 239000003002 pH adjusting agent Substances 0.000 claims description 2
- 239000007787 solid Substances 0.000 description 25
- 238000002386 leaching Methods 0.000 description 22
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 21
- 238000000034 method Methods 0.000 description 9
- 239000002562 thickening agent Substances 0.000 description 9
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- CWYNVVGOOAEACU-UHFFFAOYSA-N fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 6
- 239000003795 chemical substances by application Substances 0.000 description 5
- FYYHWMGAXLPEAU-UHFFFAOYSA-N magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 4
- 239000011777 magnesium Substances 0.000 description 4
- 229910052749 magnesium Inorganic materials 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000009854 hydrometallurgy Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 230000003472 neutralizing Effects 0.000 description 3
- 238000002203 pretreatment Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 2
- 230000004523 agglutinating Effects 0.000 description 2
- 230000005591 charge neutralization Effects 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 229940079593 drugs Drugs 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000001264 neutralization Effects 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- 125000000129 anionic group Chemical group 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003673 groundwater Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Description
本発明は、ニッケル酸化鉱石から高圧酸浸出による処理を用いたニッケルの湿式製錬方法に関し、更に詳しくは、高圧酸浸出工程に送るニッケル酸化鉱石の鉱石スラリーの前処理に関する。 The present invention relates to a method for hydrometallurgy of nickel using a treatment by high pressure acid leaching from nickel oxide ore, and more particularly to a pretreatment of an ore slurry of nickel oxide ore to be sent to a high pressure acid leaching step.
低品位ニッケル酸化鉱石からニッケルを回収する高圧酸浸出（Ｈｉｇｈ Ｐｒｅｓｓｕｒｅ Ａｃｉｄ Ｌｅａｃｈ：ＨＰＡＬ）プロセスを用いた湿式製錬方法では、高圧酸浸出工程に送られて処理される鉱石は、ニッケルを浸出しやすいように、予め解砕機や湿式篩を使用して、所定の大きさ以下に破砕および分類され、次いで水や工程水などを加えてスラリー化された、所謂鉱石スラリーを用いる。 In hydrometallurgical methods using the High Pressure Acid Leach (HPAL) process, which recovers nickel from low-grade nickel oxide ore, the ore sent to the high-pressure acid leaching process tends to leach nickel. As described above, a so-called ore slurry is used, which is crushed and classified into a predetermined size or less by using a crusher or a wet sieve in advance, and then slurried by adding water, process water, or the like.
このような鉱石スラリーは、高圧酸浸出工程における酸消費量、得られる浸出液のニッケル濃度、及びその他の不純物濃度が所定の割合となるように、数種類の酸化ニッケル鉱石をブレンドして作られることが多い。 Such an ore slurry may be made by blending several kinds of nickel oxide ores so that the acid consumption in the high-pressure acid leaching step, the nickel concentration of the obtained leachate, and the concentration of other impurities are in a predetermined ratio. many.
また鉱石スラリーでは、鉱石スラリーを構成する鉱石スラリー中の固形分（鉱石固体分）の重量割合（以下「Ｓｏｌｉｄ％」と称する）が高い（または大きいとも称す。）ほうが高圧酸浸出工程での単位時間当たりのニッケル通過量が増加することになり、相応して設備がコンパクトで済むので、投資や運転コストが低減でき、ニッケル回収効率も高くなるなど好ましい。 Further, in the ore slurry, the higher (or also referred to as, larger) the weight ratio (hereinafter referred to as “Solid%”) of the solid content (ore solid content) in the ore slurry constituting the ore slurry is the unit in the high-pressure acid leaching step. Since the amount of nickel passing per hour increases and the equipment can be made compact accordingly, investment and operating costs can be reduced, and nickel recovery efficiency is also improved, which is preferable.
しかしながら、一般的には鉱石スラリーは１０〜２０重量％と低くなることが多く、その結果高圧酸浸出工程で得られる浸出液のニッケル濃度が低く、効率的にニッケルを回収出来ないという課題があった。
このような鉱石スラリーから固液分離して高いＳｏｌｉｄ％を得ようとする場合、スラリー中の固形分の沈降速度ができるだけ大きい（速いとも称す。）ことが好ましい。
However, in general, the ore slurry is often as low as 10 to 20% by weight, and as a result, the nickel concentration of the leachate obtained in the high-pressure acid leaching step is low, and there is a problem that nickel cannot be recovered efficiently. ..
When solid-liquid separation is to be performed from such an ore slurry to obtain a high Solid%, it is preferable that the sedimentation rate of the solid content in the slurry is as high as possible (also referred to as high).
この鉱石スラリーの沈降速度を制御する方法として例えば特許文献１に示した方法がある。
特許文献１に開示される方法は、ニッケル酸化鉱石から湿式製錬方法によりニッケル等の有価金属を回収する際に、浸出工程等に固形物濃度が高い鉱石スラリーを効率的に供給するため、鉱石スラリーの沈降速度を向上させ、固液分離する際の沈降濃縮に要する時間を短縮すること、或いは鉱石スラリーの降伏応力を低下させ、流送する際の鉱石スラリーの固形物濃度を高めることができるニッケル酸化鉱石の前処理方法を提供するもので、具体的にはニッケル酸化鉱石の水性スラリーに、中和剤を添加して、ｐＨを等電点近傍に調整することにより、鉱石スラリーの沈降速度又は降伏応力を制御するものである。
As a method of controlling the sedimentation speed of this ore slurry, for example, there is a method shown in Patent Document 1.
The method disclosed in Patent Document 1 is an ore in order to efficiently supply an ore slurry having a high solid content concentration to a leaching step or the like when recovering valuable metals such as nickel from nickel oxide ore by a wet smelting method. It is possible to improve the settling speed of the slurry and shorten the time required for settling and concentrating during solid-liquid separation, or reduce the yield stress of the ore slurry and increase the solid concentration of the ore slurry when flowing. It provides a pretreatment method for nickel oxide ore. Specifically, the sedimentation rate of the ore slurry is adjusted by adding a neutralizing agent to the aqueous slurry of nickel oxide ore to adjust the pH near the isoelectric point. Or it controls the yield stress.
これを利用して、Ｓｏｌｉｄ％が低い鉱石スラリーに対しては、特許文献２に示すように、シックナーと凝集剤を利用して、鉱石スラリーのＳｏｌｉｄ％を上げる沈降濃縮（シックニング）操作を行ってから高圧酸浸出工程へ送る方法が用いられる。
特許文献２に開示された方法は、スラリー処理量を維持しつつ、固体成分率および比重の高い鉱石スラリーを製造できる鉱石スラリー製造設備および鉱石スラリー製造方法を提供するもので、具体的には原料鉱石スラリーを予備濃縮して中間鉱石スラリーを得る第１シックナー１と、中間鉱石スラリーを濃縮して濃縮鉱石スラリーを得る、第１シックナー１よりシックニング効果の高い第２シックナー２とを備える鉱石スラリー製造設備Ａ。第１シックナー１で予備濃縮された中間鉱石スラリーが第２シックナー２に供給されるので、第２シックナー２において鉱石スラリーの沈降速度が速くなり、スラリー処理量を増加できる。また、後段がシックニング効果の高い第２シックナー２であるので、固体成分率および比重の高い濃縮鉱石スラリーを製造できるものである。
Utilizing this, for an ore slurry having a low solid%, as shown in Patent Document 2, a sedimentation concentration (thickening) operation for increasing the solid% of the ore slurry is performed by using a thickener and a flocculant. Then, a method of sending to a high-pressure acid leaching process is used.
The method disclosed in Patent Document 2 provides an ore slurry production facility and an ore slurry production method capable of producing an ore slurry having a high solid component ratio and a high specific gravity while maintaining a slurry processing amount, and specifically, a raw material. An ore slurry having a first thickener 1 for pre-concentrating an ore slurry to obtain an intermediate ore slurry and a second thickener 2 for concentrating an intermediate ore slurry to obtain a concentrated ore slurry, which has a higher sickening effect than the first thickener 1. Manufacturing equipment A. Since the intermediate ore slurry pre-concentrated in the first thickener 1 is supplied to the second thickener 2, the sedimentation rate of the ore slurry in the second thickener 2 becomes high, and the slurry processing amount can be increased. Further, since the latter stage is the second thickener 2 having a high thickening effect, it is possible to produce a concentrated ore slurry having a high solid component ratio and a high specific gravity.
上記のシックニングでは、高分子炭化水素を主成分とする凝集剤を用いる。この凝集剤は、その添加量が不足するとＳｏｌｉｄ％を増加し難くなる。一方で過大に添加してもＳｏｌｉｄ％が過大に増加するものでもなく、むしろ、薬剤コストが増加し、鉱石スラリーの粘度を上昇させて設備負荷を増したり、液中の全有機炭素（ＴＯＣ）濃度を上昇させ排水処理が難しくなるなどの課題があった。 In the above sickening, a flocculant containing a high molecular weight hydrocarbon as a main component is used. If the amount of this flocculant added is insufficient, it becomes difficult to increase Solid%. On the other hand, even if it is added excessively, Solid% does not increase excessively, but rather, the drug cost increases, the viscosity of the ore slurry is increased to increase the equipment load, and the total organic carbon (TOC) in the liquid is increased. There were problems such as increasing the concentration and making wastewater treatment difficult.
さらにシックニングでは、鉱石の種類と混合割合、シックナーの形状、などの影響もあり、得られる鉱石スラリーのＳｏｌｉｄ％を安定して得るように操業することは容易でなかった。 Furthermore, in the thickening, it was not easy to operate so as to stably obtain the Solid% of the obtained ore slurry due to the influence of the type and mixing ratio of the ore, the shape of the thickener, and the like.
本発明は、高圧酸浸出工程に送るニッケル酸化鉱石のスラリー（鉱石スラリーとも称す）を製造する工程において、使用する凝集剤や中和に要する薬剤量の増加を抑制するために、鉱石スラリーの沈降速度を所定の値に制御可能なニッケル酸化鉱石スラリーの前処理方法を提供するものである。 INDUSTRIAL APPLICABILITY The present invention is to settle an ore slurry in order to suppress an increase in the amount of flocculant used and the amount of chemicals required for neutralization in the process of producing a slurry of nickel oxide ore (also referred to as an ore slurry) to be sent to a high-pressure acid leaching step. It provides a pretreatment method for a nickel oxide ore slurry whose speed can be controlled to a predetermined value.
高圧酸浸出工程に送るニッケル酸化鉱石のスラリー製造工程において、本発明者は、鋭意研究を重ねた結果、鉱石スラリーのｐＨを調整することで所定範囲のＳｏｌｉｄ％の鉱石スラリーを得る沈降速度の制御方法を完成させ、本発明に至ったものである。 In the process of producing a slurry of nickel oxide ore to be sent to a high-pressure acid leaching step, the present inventor has conducted intensive studies and controlled the sedimentation rate to obtain a Solid% ore slurry in a predetermined range by adjusting the pH of the ore slurry. The method was completed and the present invention was reached.
上記の課題を解決するための本発明の第１の発明は、ニッケル酸化鉱石を水と混合して作製したニッケル酸化鉱石スラリーと鉱酸を加圧容器に装入して高圧の加圧酸処理に付して前記ニッケル酸化鉱石スラリーからニッケルを浸出した浸出スラリーを得た後に、前記浸出スラリーを固液分離してニッケルを含有する浸出液を得る方法における前記ニッケル酸化鉱石スラリーの前処理方法において、前記ニッケル酸化鉱石スラリーを加圧容器に装入する前に、ニッケル酸化鉱石スラリーのｐＨと、前記ニッケル酸化鉱石スラリーに添加される凝集剤の重量による前記ニッケル酸化鉱石スラリーの沈降速度の挙動を予め把握し、前記加圧酸処理時に、前記加圧容器に装入されるニッケル酸化鉱石スラリーのｐＨと凝集剤の重量と沈降速度を前記把握した挙動より設定し、前記ニッケル酸化鉱石スラリーに、前記設定したニッケル酸化鉱石スラリーのｐＨになるように、ｐＨ調整剤としてサプロライト鉱石、水のいずれか、或いは両者の添加と、前記設定したニッケル酸化鉱石スラリーの沈降速度を得るための前記設定した凝集剤の重量の凝集剤の添加を行うｐＨ調整処理を実施し、次いで固液分離によるスラリー濃度調整処理に供して前記ニッケル酸化鉱石スラリーの固液分離性を調整する前処理に付すことを特徴とするニッケル酸化鉱石スラリーの前処理方法である。 In the first invention of the present invention for solving the above-mentioned problems, a nickel oxide slurry prepared by mixing nickel oxide ore with water and mineral acid are charged into a pressure vessel and treated with high-pressure pressurized acid. In the method for pretreating the nickel oxide ore slurry in the method of obtaining a leachate containing nickel by solid-liquid separation of the leachate slurry after obtaining a leachate slurry in which nickel is leached from the nickel oxide ore slurry. Before charging the nickel oxide slurry into a pressurized container, the behavior of the sedimentation rate of the nickel oxide slurry depending on the pH of the nickel oxide slurry and the weight of the flocculant added to the nickel oxide slurry is determined in advance. The pH of the nickel oxide ore slurry charged into the pressurized container, the weight of the flocculant, and the sedimentation rate are set from the grasped behavior at the time of the pressurized acid treatment, and the nickel oxide ore slurry is subjected to the above. Addition of either or both of saprolite ore or water as a pH adjuster so that the pH of the set nickel oxide ore slurry is obtained, and the above-mentioned set coagulant for obtaining the settling rate of the set nickel oxide ore slurry. The nickel oxide ore slurry is subjected to a pH adjusting treatment for adding a coagulant of the same weight as above, and then subjected to a slurry concentration adjusting treatment by solid-liquid separation to be subjected to a pretreatment for adjusting the solid-liquid separability of the nickel oxide ore slurry. This is a pretreatment method for nickel oxide ore slurry.
本発明によれば、鉱石スラリーの製造工程において、鉱石の種類や混合割合に影響されずに、鉱石スラリーの沈降速度を所定範囲に制御可能となり、ニッケル酸化鉱石スラリーのＳｏｌｉｄ％の変動を制御し、一定のＳｏｌｉｄ％の鉱石スラリーを安定して得ることができ、凝集剤や中和に用いる薬剤の増加を抑制できるものであり、工業上顕著な効果を奏するものである。 According to the present invention, in the ore slurry manufacturing process, the sedimentation rate of the ore slurry can be controlled within a predetermined range without being affected by the type and mixing ratio of the ore, and the fluctuation of Solid% of the nickel oxide ore slurry can be controlled. It is possible to stably obtain a constant Solid% ore slurry, suppress an increase in a flocculant and a chemical used for neutralization, and exert a remarkable industrial effect.
本発明は、ニッケル酸化鉱石などを高圧酸浸出するのに先立ってＳｏｌｉｄ％の高いニッケル酸化鉱石スラリーを得るために、鉱石をスラリー化した際にｐＨを調整してから固液分離に付すことで、高いＳｏｌｉｄ％のニッケル酸化鉱石スラリーを得るものである。
そのため、本発明を用いることにより常に高いＳｏｌｉｄ％のニッケル酸化鉱石スラリーを高温加圧浸出工程に送ることが出来、その結果安定したプロセスが実現できる。
In the present invention, in order to obtain a nickel oxide ore slurry having a high Solid% prior to high-pressure acid leaching of nickel oxide ore or the like, the pH of the ore is adjusted when the ore is slurried and then subjected to solid-liquid separation. , A high Solid% nickel oxide ore slurry is obtained.
Therefore, by using the present invention, a nickel oxide ore slurry having a high Solid% can always be sent to the high temperature pressure leaching step, and as a result, a stable process can be realized.
上述した原料のニッケル酸化鉱石には、表１に示すように、リモナイト（Ｌｉｍｏｎｉｔｅ）鉱やサプロライト（Ｓａｐｒｏｌｉｔｅ）鉱などのいくつかの種類があり、ニッケル湿式製錬プロセスでは、ニッケル品位や不純物品位により使い分けられる。 As shown in Table 1, there are several types of nickel oxide ores as raw materials described above, such as limonite ore and saprolite ore, and in the nickel hydrometallurgy process, depending on the nickel grade and impurity grade. It can be used properly.
ニッケル酸化鉱石を加圧酸浸出処理、即ち大気圧より高い圧力下での酸浸出である「高圧酸浸出」で処理する場合、より処理に適したリモナイト鉱を原料として用いることが多い。これは表１に示すように、リモナイト鉱はマグネシウム品位が低い特長があり、ニッケルの酸浸出に使用する硫酸がマグネシウムの浸出に利用されてロスとなる割合が低く商業的に有利なためである。 When nickel oxide ore is treated by pressure acid leaching treatment, that is, "high pressure acid leaching" which is acid leaching under a pressure higher than atmospheric pressure, limonite ore more suitable for the treatment is often used as a raw material. This is because, as shown in Table 1, limonite ore has a feature of low magnesium grade, and sulfuric acid used for acid leaching of nickel is used for magnesium leaching and the ratio of loss is low, which is commercially advantageous. ..
一方、サプロライト鉱は、ニッケル品位が高い特長があるが、上述のようにマグネシウム品位がリモナイト鉱に比較して高いために、高圧酸浸出を用いた製錬方法では、添加した硫酸がマグネシウムの浸出に消費され、硫酸ロスが多くなる短所がある。 On the other hand, saprolite ore has a feature of high nickel grade, but as described above, magnesium grade is higher than that of limonite ore. Therefore, in the smelting method using high-pressure acid leaching, the added sulfuric acid leaches magnesium. It has the disadvantage of being consumed in a large amount and increasing sulfuric acid loss.
このため、低品位ニッケル酸化鉱石からニッケルを回収する高圧酸浸出に基づく湿式製錬方法においては、高圧酸浸出工程に送られる鉱石スラリーが、所定の酸消費量、浸出液のニッケル濃度及びその他の不純物濃度となるように、リモナイト鉱やサプロライト鉱を数種類のニッケル酸化鉱石をブレンドして作られることが多かった。 Therefore, in the hydrometallurgy method based on high-pressure acid leaching that recovers nickel from low-grade nickel oxide ore, the ore slurry sent to the high-pressure acid leaching step has a predetermined acid consumption, nickel concentration in the leachate, and other impurities. It was often made by blending limonite ore and saprolite ore with several types of nickel oxide ore to achieve the concentration.
また、高圧酸浸出工程に送られる鉱石スラリーは、高圧酸浸出工程への単位時間当たりのニッケル通過量を増加させ高い生産性を実現するために、できるだけＳｏｌｉｄ％が高いことが求められる。 Further, the ore slurry sent to the high-pressure acid leaching step is required to have as high a Solid% as possible in order to increase the amount of nickel passing through the high-pressure acid leaching step per unit time and realize high productivity.
高いＳｏｌｉｄ％を得るために固液分離時に凝集剤を用いるが、凝集剤の最適な添加量を選定することは容易でなく添加が不足すると固液分離が不完全となり、過剰に添加すると薬剤コストが増加するだけではなく、凝集剤の主成分が高分子炭化水素であるために、鉱石スラリーの粘度を過度に増加させたり、鉱石スラリーの液中のＣ品位の上昇をもたらす懸念がある。 A flocculant is used at the time of solid-liquid separation in order to obtain a high solid%, but it is not easy to select the optimum amount of the flocculant to be added. However, since the main component of the flocculant is a high molecular weight hydrocarbon, there is a concern that the viscosity of the ore slurry may be excessively increased or the C grade in the liquid of the ore slurry may be increased.
そこで本発明者は、凝集剤の添加量と沈降速度とｐＨの影響から最適な添加量を選定する方法を用いた。
この方法の場合には、鉱石スラリーのｐＨが異なると凝集剤添加量が大きく異なるため、できる限り事前にｐＨ調整することが重要となる。
Therefore, the present inventor used a method of selecting the optimum addition amount from the influence of the addition amount of the flocculant, the sedimentation rate and the pH.
In the case of this method, it is important to adjust the pH in advance as much as possible because the amount of the flocculant added differs greatly depending on the pH of the ore slurry.
また、ｐＨ調整に用いる中和剤の選定により沈降速度に影響があることも見出している。
つまり、同じｐＨであっても水酸化ナトリウムなどの薬剤を用いて調整した場合よりも、上記のサプロライト鉱などの鉱石や元来ｐＨが高い水などを用いて調整した場合の方が、凝集剤の効果が発揮でき、より大きな沈降速度が得られることを見出した。
このことは、水酸化ナトリウムなどの薬剤の場合、スラリー中の液部分の塩濃度が過度の上昇を示すことで、凝集剤の効果がそれだけ弱められたと考えられる。
It has also been found that the sedimentation rate is affected by the selection of the neutralizing agent used for pH adjustment.
In other words, even if the pH is the same, the flocculant is more likely to be adjusted using the above-mentioned ore such as saprolite ore or water that originally has a high pH than when adjusted using a chemical such as sodium hydroxide. It was found that the effect of the above can be exhibited and a larger sedimentation rate can be obtained.
This is considered to be because, in the case of a drug such as sodium hydroxide, the effect of the flocculant was weakened by the excessive increase in the salt concentration of the liquid portion in the slurry.
なお、上記「ｐＨが高い水」として具体的には、鉱石スラリーを調製する際に用いる水として河川から採取した水を使うことが多いが、これに工程内で生じた排水を繰り返し、適宜混合した水などがある。また地下水などアルカリ性の土壌から採取した水などが挙げられる。
以上述べてきた方法を用いることにより、本発明では凝集剤の添加量を最適に管理すると同時に高い沈降速度を得ることを実現するもので、以下に具体例を用いて説明する。
Specifically, as the above-mentioned "water having a high pH", water collected from a river is often used as water used when preparing an ore slurry, but the wastewater generated in the process is repeated and mixed appropriately. There is water etc. In addition, water collected from alkaline soil such as groundwater can be mentioned.
By using the method described above, in the present invention, it is possible to optimally control the amount of the flocculant added and at the same time obtain a high sedimentation rate, which will be described below using specific examples.
［鉱石スラリーの沈降速度に及ぼすスラリーｐＨの影響］
ニッケル酸化鉱石として、表１に示したリモナイト鉱を破砕し、スラリー濃度が４重量％になるように純水で希釈した鉱石スラリーを作製し、この鉱石スラリーのｐＨは５．６だった。これに水酸化ナトリウム溶液を添加してｐＨを５．８と６．０に調整した。
上記２試料の調整済鉱石スラリーと、水酸化ナトリウムを添加しなかった場合を含めた３試料に、アニオン性凝集剤である栗田工業株式会社製の商品名ＰＡ８３４を、スラリー中での濃度が０．０３重量％になるように添加し、固液分離させた。この際の鉱石スラリーが固液分離し、固形分が沈降する際の固形分の上端の移動速度を記録し、１時間当たりの沈降速度に換算し、この値を沈降速度［ｍ・ｈ−１］とした。
[Effect of slurry pH on ore slurry sedimentation rate]
As the nickel oxide ore, the limonite ore shown in Table 1 was crushed to prepare an ore slurry diluted with pure water so that the slurry concentration was 4% by weight, and the pH of this ore slurry was 5.6. A sodium hydroxide solution was added thereto to adjust the pH to 5.8 and 6.0.
Kurita Water Industries, Ltd.'s trade name PA834, which is an anionic flocculant, was added to the three samples including the adjusted ore slurry of the above two samples and the case where sodium hydroxide was not added, and the concentration in the slurry was 0. It was added so as to be 0.03% by weight, and the mixture was separated into solid and liquid. At this time, the ore slurry is solid-liquid separated, and the moving speed of the upper end of the solid content when the solid content is settled is recorded, converted into the settling speed per hour, and this value is converted into the settling speed [m · h -1. ].
その結果を図１に示す。図１において、横軸（Ｆｌｏｃｃｕｌａｎｔ ｄｏｓａｇｅ、Ｆｆｌｏｃ／ｇ・ｔ−１）は鉱石１トン当たりの凝集剤添加量［ｇｒ］を示し、縦軸（Ｓｅｔｔｌｉｎｇ ｒａｔｅ、Ｒ／ｍ・ｈ−１）は単位時間当たりの沈降距離［ｍ］で示す沈降速度［ｍ・ｈ−１］である。 The results are shown in FIG. In FIG. 1, the horizontal axis (Flocculant dose, Ffloc / g · t -1 ) indicates the amount of flocculant added per ton of ore [gr], and the vertical axis (Settling rate, R / m · h -1 ) is. It is a settling speed [m · h -1 ] indicated by a settling distance [m] per unit time.
図１に示すように、ｐＨ５．６〜６．０の範囲では、凝集剤の添加量が増加するとともに沈降速度が大きくなる。しかし、ある添加量以上では沈降速度はほぼ一定となる。また、凝集剤を添加する前の鉱石スラリーのｐＨが低いほど、同じ沈降速度を得るために必要な凝集剤の量は増加する。
すなわち図１の条件の場合、ｐＨを６．０に調整し、凝集剤をスラリー中の鉱石１トン当たり８０ｇ程度添加することで、最低の凝集剤添加量で最も高い沈降速度、すなわち固液分離性が得られることになる。
As shown in FIG. 1, in the range of pH 5.6 to 6.0, the amount of the flocculant added increases and the sedimentation rate increases. However, the sedimentation rate becomes almost constant above a certain amount of addition. Also, the lower the pH of the ore slurry before adding the flocculant, the greater the amount of flocculant required to obtain the same sedimentation rate.
That is, in the case of the conditions shown in FIG. 1, by adjusting the pH to 6.0 and adding about 80 g of the agglutinating agent per ton of ore in the slurry, the highest sedimentation rate with the minimum amount of the agglutinating agent added, that is, solid-liquid separation. Sex will be obtained.
このようにｐＨと沈降速度の関係をあらかじめ把握しておくことで、最適な沈降速度を最低限の凝集剤添加量で実現できる。 By grasping the relationship between pH and sedimentation rate in advance in this way, the optimum sedimentation rate can be realized with the minimum amount of coagulant added.
［ｐＨ調整方法と沈降速度との関係］
上記と同じ鉱石スラリーを用意し、これに中和剤として水酸化ナトリウムや表１に示す組成のサプロライト鉱石を粉砕したものを添加してｐＨを調整し、上記と同じ凝集剤、添加量を添加して沈降速度を測定した。
その結果を図２に示す。図２において、横軸、縦軸共に図１と同じである。
[Relationship between pH adjustment method and sedimentation rate]
Prepare the same ore slurry as above, add sodium hydroxide or crushed saprolite ore having the composition shown in Table 1 as a neutralizing agent to adjust the pH, and add the same flocculant and addition amount as above. Then, the settling speed was measured.
The results are shown in FIG. In FIG. 2, both the horizontal axis and the vertical axis are the same as those in FIG.
図２に示すように、サプロライト鉱を添加して鉱石スラリーのｐＨを６．０に調整した場合（図２の黒四角／■）、同じｐＨ６．０でも水酸化ナトリウムを添加して調整した場合（図２の黒三角／▲）に比べて大きな沈降速度が得られた。
また、サプロライト鉱の添加量が１０％と２０％ではｐＨの差が０．１程度でも沈降速度に大きな差が生じた。（図２の黒丸／●：１０％と黒四角／■：２０％）
さらに、元々ｐＨが６．２である水を用いた場合（図２での×）は、水酸化ナトリウムやサプロライト鉱を用いた場合に比較して、大きい沈降速度が得られる。
As shown in FIG. 2, when the pH of the ore slurry is adjusted to 6.0 by adding saprolite ore (black square in FIG. 2 / ■), when the pH is adjusted to 6.0 by adding sodium hydroxide. A larger settling speed was obtained as compared with (black triangle / ▲ in FIG. 2).
Further, when the amount of saprolite ore added was 10% and 20%, a large difference in sedimentation rate occurred even if the difference in pH was about 0.1. (Black circle in Fig. 2 / ●: 10% and black square / ■: 20%)
Furthermore, when water originally having a pH of 6.2 is used (x in FIG. 2), a large sedimentation rate can be obtained as compared with the case where sodium hydroxide or saprolite ore is used.
このようにｐＨの調整にサプロライト鉱やｐＨが高い水を用いることにより、より少ない凝集剤で大きな沈降速度を得ることができることを見出した。 As described above, it has been found that by using saprolite ore or water having a high pH for adjusting the pH, a large sedimentation rate can be obtained with a smaller amount of coagulant.
Claims (1)
前記ニッケル酸化鉱石スラリーの加圧容器に装入する前に、
ニッケル酸化鉱石スラリーのｐＨと、前記ニッケル酸化鉱石スラリーに添加される凝集剤の重量による前記ニッケル酸化鉱石スラリーの沈降速度の挙動を予め把握し、前記加圧酸処理時に、前記加圧容器に装入されるニッケル酸化鉱石スラリーのｐＨと凝集剤の重量と沈降速度を前記把握した挙動より設定し、
前記ニッケル酸化鉱石スラリーに、前記設定したニッケル酸化鉱石スラリーのｐＨになるように、ｐＨ調整剤としてサプロライト鉱石、水のいずれか、或いは両者の添加と、前記設定したニッケル酸化鉱石スラリーの沈降速度を得るための前記設定した凝集剤の重量の凝集剤の添加を行うｐＨ調整処理を実施し、
次いで固液分離によるスラリー濃度調整処理に供して前記ニッケル酸化鉱石スラリーの固液分離性を調整する前処理に付すことを特徴とするニッケル酸化鉱石スラリーの前処理方法。 The nickel oxide ore slurry prepared by mixing nickel oxide ore with water and the ore acid were charged into a pressurized container and subjected to pressure acid treatment to obtain a leached slurry in which nickel was leached from the nickel oxide ore slurry. Later, in the method for pretreating the nickel oxide ore slurry in the method of solid-liquid separating the leachate slurry to obtain a nickel-containing leachate.
Before charging the pressure vessel of the nickel oxide ore slurry,
The behavior of the sedimentation rate of the nickel oxide ore slurry depending on the pH of the nickel oxide ore slurry and the weight of the flocculant added to the nickel oxide ore slurry is grasped in advance, and the nickel oxide ore slurry is loaded in the pressurized container during the pressurized acid treatment. The pH of the nickel oxide ore slurry to be added, the weight of the flocculant, and the sedimentation rate are set from the above-mentioned behavior.
Add either or both of saprolite ore or water as a pH adjuster to the nickel oxide ore slurry so that the pH of the nickel oxide ore slurry is set, and the settling rate of the nickel oxide ore slurry. A pH adjustment treatment was carried out in which the coagulant was added in the weight of the coagulant set above to obtain the oil.
Next, a method for pretreating a nickel oxide ore slurry, which is subjected to a slurry concentration adjusting treatment by solid-liquid separation and subjected to a pretreatment for adjusting the solid-liquid separability of the nickel oxide ore slurry.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2019168541A JP7057900B2 (en) | 2019-09-17 | 2019-09-17 | Pretreatment method for nickel oxide ore slurry |
| PCT/JP2020/034287 WO2021054240A1 (en) | 2019-09-17 | 2020-09-10 | Pretreatment method for nickel oxide ore slurry |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2019168541A JP7057900B2 (en) | 2019-09-17 | 2019-09-17 | Pretreatment method for nickel oxide ore slurry |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| JP2021046572A JP2021046572A (en) | 2021-03-25 |
| JP2021046572A5 true JP2021046572A5 (en) | 2022-01-04 |
| JP7057900B2 JP7057900B2 (en) | 2022-04-21 |
Family
ID=74877869
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2019168541A Active JP7057900B2 (en) | 2019-09-17 | 2019-09-17 | Pretreatment method for nickel oxide ore slurry |
Country Status (2)
| Country | Link |
|---|---|
| JP (1) | JP7057900B2 (en) |
| WO (1) | WO2021054240A1 (en) |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2320781A1 (en) * | 1975-08-14 | 1977-03-11 | Nickel Sln Ste Metallurg Le | PROCESS FOR PRECONCENTRING NICKEL-OXIDIZED OXIDES OF LATERITIC ORIGIN |
| JPH08112585A (en) * | 1994-08-25 | 1996-05-07 | Shinko Kagaku Kogyo Kk | Treatment of dust-collector ash |
| EP1929056A4 (en) * | 2005-09-30 | 2009-04-15 | Bhp Billiton Innovation Pty | Process for leaching lateritic ore at atmospheric pressure |
| JP2019044208A (en) * | 2017-08-30 | 2019-03-22 | 住友金属鉱山株式会社 | Ore slurry concentration method in nickel oxide ore refining |
-
2019
- 2019-09-17 JP JP2019168541A patent/JP7057900B2/en active Active
-
2020
- 2020-09-10 WO PCT/JP2020/034287 patent/WO2021054240A1/en active Application Filing
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2013077296A1 (en) | Method for producing high-purity nickel sulfate | |
| JP2007297717A (en) | Method for recovering copper from sulfide ore material using high temperature pressure leaching, solvent extraction and electrowinning | |
| JP5360243B2 (en) | Thickener device in ore slurry manufacturing process and method for controlling solid component ratio | |
| AU2013236726B2 (en) | Method for producing hematite for iron production | |
| JP5692458B1 (en) | Solid-liquid separation treatment method and nickel oxide ore hydrometallurgy method | |
| JP2019044208A (en) | Ore slurry concentration method in nickel oxide ore refining | |
| JP5790839B2 (en) | Chromite recovery method | |
| PH12018000170A1 (en) | Solid-liquid separation process of nickel high pressure leached residue | |
| JP5971364B1 (en) | Ore slurry pretreatment method, ore slurry production method | |
| JP7057900B2 (en) | Pretreatment method for nickel oxide ore slurry | |
| JP2017133050A (en) | Method for recovering scandium | |
| JP2021046572A5 (en) | ||
| CN110036123A (en) | The method for controlling iron via the formation of magnetic iron ore in hydrometallurgical processes | |
| JP5692313B2 (en) | Thickener device in ore slurry manufacturing process and method for controlling solid component ratio | |
| WO2016088240A1 (en) | Apparatus for producing ore slurry and process for producing ore slurry | |
| JP7279546B2 (en) | Nickel oxide ore leaching method and hydrometallurgical method including the same | |
| Lopez et al. | Copper and cyanide recovery from barren leach solution at the gold processing plant | |
| JP7112677B2 (en) | Selective Cobalt Leaching Method | |
| JP2021176981A (en) | Method for managing thickener for obtaining high-concentration slurry | |
| JP5811297B1 (en) | Ore slurry manufacturing equipment and ore slurry manufacturing method | |
| JP2011058018A (en) | Method for recovering gold concentrate from leach residue of copper sulfide minerals | |
| WO2022118743A1 (en) | Method for preparing nickel oxide ore slurry | |
| JP2020033602A (en) | Method of manufacturing high concentration ore slurry | |
| JP5783223B2 (en) | Ore slurry manufacturing equipment and ore slurry manufacturing method | |
| JP7127679B2 (en) | Method for producing ore slurry, hydrometallurgical method for nickel oxide ore |