CN218932247U - System for recycling nickel from solution containing low-concentration nickel through centrifugal extraction - Google Patents
System for recycling nickel from solution containing low-concentration nickel through centrifugal extraction Download PDFInfo
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Abstract
The utility model discloses a system for centrifugally extracting and recycling nickel from a solution containing low concentration nickel, which comprises a centrifugal extraction unit, a centrifugal back extraction unit, a nickel recycling feed liquid storage tank, an organic phase storage tank, a nickel recycling back liquid storage tank, a nickel recycling residual liquid storage tank, a back acid storage tank, an organic feed pump, a pipeline mixer, a heat exchanger and a saponifier storage tank. The system of the utility model is used for centrifugally extracting and recovering nickel from the solution containing low-concentration nickel, has small acid and alkali consumption, can realize continuous production, has high recovery rate of nickel which is more than 99 percent, has high purity of recovered nickel which reaches 99.0 percent, and can be directly used for subsequent production; meanwhile, the amount of generated wastewater is small, and the subsequent wastewater treatment pressure is greatly reduced. The organic phase input amount of the system is only 1/30-1/10 of that of the box-type extraction process.
Description
Technical field:
the utility model relates to a system for recovering nickel by centrifugal extraction, in particular to a system for recovering nickel by centrifugal extraction from a solution containing low-concentration nickel.
The background technology is as follows:
the extraction method is an important processing means for cobalt-nickel separation, extraction and purification. However, it is inevitable that a lot of waste liquid containing low concentration of nickel is generated during cobalt-nickel extraction separation. Such as nickel soap wastewater, cobalt raffinate, running-off drip recovery solution, etc. Such solutions are generally characterized as having high sodium and low nickel content, and many solutions also contain small or trace amounts of other elements (e.g., cobalt, magnesium, calcium, manganese, etc.). At present, a precipitation method or an adsorption method is generally used for enriching and recovering valuable elements. The precipitation method adopts hydroxide to precipitate nickel ions to generate nickel hydroxide, part of other metal ions in waste liquid are precipitated at the same time, sulfuric acid is used for dissolving the nickel ions during purification, nickel exists in the form of nickel sulfate, and other impurity ions also enter the solution. Patent CN2011102114516 discloses a treatment method for recovering nickel from nickel-containing waste liquid, which adopts the working processes of ion exchange tree adsorption, then analysis and the like to recover nickel from the nickel-containing waste liquid, and has high yield, and the nickel content of the adsorbed waste liquid is as low as below 2mg/L and then is discharged. Although the adsorption effect is good, the adsorption capacity of the adsorbent is limited, frequent adsorption washing and desorption are needed when the nickel concentration is high, and the amount of wastewater generated by washing and desorption is large. The purity of the nickel recovered by the two methods depends on the types and the contents of impurity elements in the waste liquid, and the method has the advantages of more production steps, low efficiency, low nickel recovery rate and high recovery production cost. There is a method for recovering nickel by using a box type extraction tank at present, but the method has the problems of large occupied area, large solution pressure tank quantity, large input quantity of organic phase, low recovery speed and the like.
The utility model comprises the following steps:
in order to solve the technical problems, the utility model aims to provide a simple and efficient system for centrifugally extracting and recycling nickel from a solution containing low-concentration nickel.
The utility model is implemented by the following technical scheme: a system for centrifugally extracting and recycling nickel from a solution containing low-concentration nickel comprises a centrifugal extraction unit, a centrifugal back extraction unit, a nickel recycling feed liquid storage tank, an organic phase storage tank, a nickel recycling back liquid storage tank, a nickel recycling residual liquid storage tank, a back acid storage tank, an organic feed pump, a pipeline mixer, a heat exchanger and a saponification agent storage tank;
the outlet of the saponification agent storage tank and the discharge port of the organic phase storage tank are connected with the inlet of the organic feed pump through pipelines; the outlet of the organic feed pump is connected with the inlet of the pipeline mixer, and the outlet of the pipeline mixer is connected with the material inlet of the heat exchanger through a pipeline; as the organic phase is acidic and reacts with alkali liquor such as aqueous ammonia or sodium hydroxide solution and the like, the reaction speed is high, the saponification reaction can be completed in a pipeline mixer, the saponification reaction can be completed while the organic phase is fully mixed with the saponification agent by utilizing the pipeline mixer, and meanwhile, the equipment occupies small space and is low in cost. The organic phase reacts with the saponifying agent to release heat, and the temperature of the saponified organic phase is reduced by the heat exchanger, so that the temperature in the system is controlled below 55 ℃, and the waste and the influence on the environment caused by volatilization of the organic phase are avoided.
The material outlet of the heat exchanger is connected with the organic phase inlet of the first centrifugal extractor of the centrifugal extraction unit through a pipeline; the loaded organic phase outlet of the tail-stage centrifugal extractor of the centrifugal extraction unit is connected with the loaded organic phase inlet of the head-stage stripping centrifugal extractor of the centrifugal stripping unit through a pipeline; the organic phase outlet of the tail stage stripping centrifugal extractor of the centrifugal stripping unit is connected with the feed inlet of the organic phase storage tank through a pipeline;
the discharge port of the nickel recovery feed liquid storage tank is connected with the feed liquid inlet of the tail table centrifugal extractor of the centrifugal extraction unit through a pipeline; the raffinate outlet of the first centrifugal extractor of the centrifugal extraction unit is connected with the inlet of the nickel recovery raffinate storage tank through a pipeline;
the outlet of the acid reversing storage tank is connected with the acid inlet of the tail stage stripping centrifugal extractor of the centrifugal stripping unit through a pipeline; and a nickel-loaded reverse liquid outlet of the first stripping centrifugal extractor of the centrifugal reverse extraction unit is connected with an inlet of the nickel recovery reverse liquid storage tank through a pipeline.
Further, the centrifugal extraction unit comprises at least one centrifugal extraction machine, and when the centrifugal extraction unit comprises two or more than two centrifugal extraction machines, the loaded organic phase outlet of the former centrifugal extraction machine of the two adjacent centrifugal extraction machines is connected with the organic phase inlet of the latter centrifugal extraction machine through a pipeline; the raffinate outlet of the last centrifugal extractor of the two adjacent centrifugal extractors is connected with the feed liquid inlet of the previous centrifugal extractor through a pipeline.
Further, the centrifugal stripping unit comprises at least one stripping centrifugal extractor, and when the centrifugal stripping unit comprises two or more than two stripping centrifugal extractors, the loaded organic phase outlet of the former stripping centrifugal extractor of the two adjacent stripping centrifugal extractors is connected with the loaded organic phase inlet of the latter stripping centrifugal extractor through a pipeline; the nickel-loaded counter-liquid outlet of the back-extraction centrifugal extractor of the two adjacent counter-extraction centrifugal extractors is connected with the acid inlet of the front-extraction centrifugal extractor through a pipeline.
Further, the system for recovering nickel from extraction also comprises a backwashing unit, wherein a loaded organic phase outlet of a tail stage centrifugal extractor of the centrifugal extraction unit is connected with a loaded organic phase inlet of a head stage backwashing centrifugal extractor of the backwashing unit through a pipeline, and a loaded organic phase outlet of the tail stage backwashing centrifugal extractor of the backwashing unit is connected with a loaded organic phase inlet of a head stage stripping centrifugal extractor of the centrifugal stripping unit through a pipeline; the outlet of the acid-back storage tank is connected with the acid inlet of the back washing centrifugal extractor of the tail table of the back washing unit through a pipeline; and a backwash liquid outlet of the first backwash centrifugal extractor of the backwash unit is connected with a feed liquid inlet of the tail centrifugal extractor of the centrifugal extraction unit through a pipeline.
Further, the backwashing unit comprises at least one backwashing centrifugal extractor, and when the backwashing centrifugal extractor comprises two or more backwashing centrifugal extractors, the loaded organic phase outlet of the former backwashing centrifugal extractor of the two adjacent backwashing centrifugal extractors is connected with the loaded organic phase inlet of the latter backwashing centrifugal extractor through a pipeline; the backwash liquid outlet of the back backwash centrifugal extractor of the two adjacent backwash centrifugal extractors is connected with the acid inlet of the front backwash centrifugal extractor through a pipeline.
Further, the system for centrifugally extracting and recycling nickel from the low-concentration nickel-containing solution further comprises a saponifier flowmeter, wherein an outlet of the saponifier storage tank is connected with an inlet of the saponifier flowmeter through a pipeline, and an outlet of the saponifier flowmeter and a discharge port of the organic phase storage tank are connected with an inlet of the organic feed pump through a pipeline; the saponifier flowmeter is a volumetric flowmeter.
Further, the system for centrifugally extracting and recycling nickel from the solution containing low-concentration nickel further comprises a first acid-reversing flowmeter, wherein an outlet of the acid-reversing storage tank is connected with an inlet of the first acid-reversing flowmeter through a pipeline, and an outlet of the first acid-reversing flowmeter is connected with an acid inlet of a final-stage stripping centrifugal extractor of the centrifugal stripping unit through a pipeline; the first counter acid flowmeter is a volumetric flowmeter.
Further, the system for centrifugally extracting and recycling nickel from the low-concentration nickel-containing solution further comprises a second acid-reflecting flowmeter, wherein the outlet of the acid-reflecting storage tank is connected with the inlet of the second acid-reflecting flowmeter through a pipeline; the outlet of the second acid-back flowmeter is connected with the acid inlet of the back washing centrifugal extractor of the tail table of the back washing unit through a pipeline; the second acid counter flowmeter is a volumetric flowmeter.
The utility model has the advantages that:
(1) The system of the utility model is used for centrifugally extracting and recovering nickel from the solution containing low-concentration nickel, has small acid and alkali consumption, can realize continuous production, has high recovery rate of nickel which is more than 99 percent, has high purity of recovered nickel which reaches 99.0 percent, and can be directly used for subsequent production; meanwhile, the amount of generated wastewater is small, and the subsequent wastewater treatment pressure is greatly reduced.
(2) Compared with box type extraction, the centrifugal extraction system has the advantages of high separation speed, short stage retention time, rapid phase separation, high extraction efficiency and great improvement of production efficiency.
(3) The main equipment of the system is a centrifugal extractor, the equipment is small in volume, the occupied area and the operation space are saved, and the total occupied area is 1/3 of the box-type extraction; according to the calculation of the volumes of the mixing chamber, the clarifying chamber and the rotary drum of the centrifugal extractor of the box type extraction tank, the organic phase input amount of the system is only 1/30-1/10 of that of the box type extraction process, so that the organic phase input amount is greatly reduced, and the raw material cost is reduced.
(4) The sealing performance is good, and the working environment is good.
(5) The operation performance is good, and continuous uninterrupted operation can be realized.
Description of the drawings:
in order to more clearly illustrate the embodiments of the utility model or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the utility model, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a system for recovering nickel from a solution containing nickel at low concentration in accordance with example 1.
FIG. 2 is a schematic diagram of a system for recovering nickel from a low concentration nickel containing solution by centrifugal extraction in example 2.
The drawings are as follows:
the device comprises a head centrifugal extractor 1, a tail centrifugal extractor 2, a head back-extraction centrifugal extractor 3, a tail back-extraction centrifugal extractor 4, a saponifying agent storage tank 5, a saponifying agent flowmeter 6, an organic phase storage tank 7, an organic feed pump 8, a pipeline mixer 9, a heat exchanger 10, a nickel recovery feed liquid storage tank 11, a nickel recovery residual liquid storage tank 12, a back-acid storage tank 13, a first back-acid flowmeter 14, a nickel recovery back-liquid storage tank 15, a head back-washing centrifugal extractor 16, a tail back-washing centrifugal extractor 17 and a second back-acid flowmeter 18.
The specific embodiment is as follows:
the following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
The centrifugal extractor, the back extraction centrifugal extractor and the back washing centrifugal extractor related in the following embodiments are all centrifugal extractors with model numbers CTL-500FC manufactured by Baotou Shibo rare earth extraction equipment limited company; the patent number is ZL200620167754.7.
The saponifier flowmeter, the first acid counter flowmeter and the second acid counter flowmeter in the following embodiments are all volumetric flowmeters, and the volumetric flowmeters are independently researched and developed by Baotou Shibo rare earth extraction equipment limited company, and have the patent number ZL202122315035.2.
Example 1: a system for centrifugally extracting and recycling nickel from a solution containing low concentration nickel, which comprises a centrifugal extraction unit, a centrifugal back extraction unit, a nickel recycling feed liquid storage tank 11, an organic phase storage tank 7, a nickel recycling back liquid storage tank 15, a nickel recycling residual liquid storage tank 12, a back acid storage tank 13, an organic feed pump 8, a pipeline mixer 9, a heat exchanger 10, a saponifying agent storage tank 5, a saponifying agent flow meter 6, a first back acid flow meter 14 and a second back acid flow meter 18;
in the embodiment, the centrifugal extraction unit comprises 2 centrifugal extractors, namely a head centrifugal extractor 1 and a tail centrifugal extractor 2;
in this embodiment, the centrifugal stripping unit includes 2 stripping centrifugal extractors, namely a first stripping centrifugal extractor 3 and a last stripping centrifugal extractor 4.
The outlet of the saponifying agent storage tank 5 is connected with the inlet of the saponifying agent flowmeter 6 through a pipeline, and the outlet of the saponifying agent flowmeter 6 and the discharge port of the organic phase storage tank 7 are connected with the inlet of the organic feed pump 8 through a pipeline; the outlet of the organic feed pump 8 is connected with the inlet of the pipeline mixer 9, and the outlet of the pipeline mixer 9 is connected with the material inlet of the heat exchanger 10 through a pipeline; since the organic phase (the organic phase in this embodiment is composed of P507 and white oil) is acidic and reacts with an alkali solution such as aqueous ammonia or sodium hydroxide solution, the reaction speed is high, the saponification reaction can be completed in the pipe mixer 9, the saponification reaction can be completed while the organic phase is fully mixed with the saponification agent by using the pipe mixer 9, and meanwhile, the equipment occupation space is small and the cost is low. The organic phase reacts with the saponifying agent to release heat, and the temperature of the saponified organic phase is reduced by the heat exchanger 10, so that the temperature in the system is controlled below 55 ℃, and the waste and the influence on the environment caused by volatilization of the organic phase are avoided.
The material outlet of the heat exchanger 10 is connected with the organic phase inlet of the first centrifugal extractor 1 through a pipeline; the loaded organic phase outlet of the first centrifugal extractor 1 is connected with the organic phase inlet of the tail centrifugal extractor 2 through a pipeline; the loaded organic phase outlet of the tail centrifugal extractor 2 is connected with the loaded organic phase inlet of the head counter-extraction centrifugal extractor 3 through a pipeline; the loaded organic phase outlet of the head counter extraction centrifugal extractor 3 is connected with the loaded organic phase inlet of the tail counter extraction centrifugal extractor 4 through a pipeline; the organic phase outlet of the tail stage back extraction centrifugal extractor 4 is connected with the feed inlet of the organic phase storage tank 7 through a pipeline;
the discharge port of the nickel recovery feed liquid storage tank 11 is connected with the feed liquid inlet of the tail table centrifugal extractor 2 through a pipeline; the raffinate outlet of the tail centrifugal extractor 2 is connected with the feed liquid inlet of the head centrifugal extractor 1 through a pipeline; the raffinate outlet of the first centrifugal extractor 1 is connected with the inlet of the nickel recovery raffinate storage tank 12 through a pipeline.
The outlet of the acid return storage tank 13 is connected with the inlet of the first acid return flowmeter 14 through a pipeline, and the outlet of the first acid return flowmeter 14 is connected with the acid inlet of the tail stage stripping centrifugal extractor 4 through a pipeline; the nickel-loaded reverse liquid outlet of the tail counter stripping centrifugal extractor 4 is connected with the acid inlet of the head counter stripping centrifugal extractor 3 through a pipeline; the nickel-loaded reverse liquid outlet of the first stripping centrifugal extractor 3 is connected with the inlet of a nickel recovery reverse liquid storage tank 15 through a pipeline.
The working process is described as follows:
the organic phase in the organic phase storage tank 7 and the saponifier in the saponifier storage tank 5 are pumped into the pipeline mixer 9 by the organic feed pump 8, the organic phase and the saponifier are fully mixed in the pipeline mixer 9, saponification reaction occurs at the same time, the saponified organic phase is pumped into the first centrifugal extractor 1 after heat exchange and cooling with system cooling water by the heat exchanger 10, the liquid after the first centrifugal extraction is carried out with the liquid from the tail centrifugal extractor 2, the loaded organic phase after the second centrifugal extraction enters the tail centrifugal extractor 2, the liquid after the first centrifugal extraction is carried out with the liquid from the nickel recovery liquid storage tank 11, the loaded organic phase after the first centrifugal extraction enters the first centrifugal extractor 3, the strip liquid after the first centrifugal extraction is carried out with the strip centrifugal extractor 4, the loaded organic phase after the second centrifugal extraction enters the tail centrifugal extractor 4, the blank organic phase after the first centrifugal extraction is carried out with sulfuric acid or hydrochloric acid from the acid storage tank 13, and the organic phase after the first centrifugal extraction is recycled; after the primary centrifugal extraction and the secondary centrifugal extraction are carried out on the feed liquid from the nickel recovery feed liquid storage tank 11, the residual liquid after nickel recovery is pumped into the nickel recovery residual liquid storage tank 12 through the first centrifugal extractor 1 for the subsequent wastewater treatment process.
The back extraction liquid after the first-stage back extraction centrifugal extraction and the second-stage back extraction centrifugal extraction is pumped into a nickel recovery back liquid storage tank 15 through a first back extraction centrifugal extractor 3, and the back extraction liquid can be separated according to the content of each element or can be directly used for producing nickel sulfate products.
Example 2: unlike the embodiment 1, the system for centrifugally extracting and recovering nickel from the solution containing low concentration nickel further comprises a backwashing unit, wherein the backwashing unit comprises 2 backwashing centrifugal extractors, namely a head backwashing centrifugal extractor 16 and a tail backwashing centrifugal extractor 17.
The loaded organic phase outlet of the tail table centrifugal extractor 2 is connected with the loaded organic phase inlet of the head table backwash centrifugal extractor 16 through a pipeline, and the loaded organic phase outlet of the head table backwash centrifugal extractor 16 is connected with the loaded organic phase inlet of the tail table backwash centrifugal extractor 17 through a pipeline; the loaded organic phase outlet of the tail counter-washing centrifugal extractor 17 is connected with the loaded organic phase inlet of the head counter-washing centrifugal extractor 3 through a pipeline;
the outlet of the acid-reflecting storage tank 13 is connected with the inlet of the second acid-reflecting flowmeter 18 through a pipeline; the outlet of the second acid-return flowmeter 18 is connected with the acid inlet of the tail table backwashing centrifugal extractor 17 through a pipeline; the backwash liquid outlet of the tail table backwash centrifugal extractor 17 is connected with the acid inlet of the head table backwash centrifugal extractor 16 through a pipeline; the backwash liquid outlet of the head backwash centrifugal extractor 16 is connected with the feed liquid inlet of the tail centrifugal extractor 2 through a pipeline.
The working process is described as follows:
the working procedure is different from that of example 1 in that: the loaded organic phase after the first-stage centrifugal extraction enters a first-stage backwashing centrifugal extractor 16, and is subjected to second-stage backwashing with backwashing liquid from a tail-stage backwashing centrifugal extractor 17 after the first-stage backwashing, and the loaded organic phase after the backwashing enters the tail-stage backwashing centrifugal extractor 17, and enters a first-stage back-extraction centrifugal extractor 3 after being subjected to the first-stage backwashing with sulfuric acid or hydrochloric acid from a back-acid storage tank 13. The sulfuric acid or hydrochloric acid from the acid storage tank 13 is subjected to primary backwashing and secondary backwashing, and the reverse washing liquid and the feed liquid from the nickel recovery feed liquid storage tank 11 are pumped into the tail table centrifugal extractor 2 together for primary centrifugal extraction.
In the embodiment, the feed liquid is nickel soap wastewater of a nickel sulfate impurity removal line, and the nickel content is 2g/L. After the material liquid is centrifugally extracted and back extracted by the system of the embodiment, the residual liquid after nickel recovery and the back extraction liquid are subjected to component analysis, wherein the nickel content in the residual liquid after nickel recovery is less than 0.02g/L, and the nickel content in the back extraction liquid is 100g/L. The residual liquid after nickel recovery is discharged to wastewater treatment, and the back extraction liquid can be directly used for producing nickel sulfate products, the purity of the back extraction liquid reaches 99.0%, and the yield of nickel is 99%.
The foregoing description of the preferred embodiments of the utility model is not intended to be limiting, but rather is intended to cover all modifications, equivalents, alternatives, and improvements that fall within the spirit and scope of the utility model.
Claims (8)
1. The system for centrifugally extracting and recycling nickel from the low-concentration nickel-containing solution is characterized by comprising a centrifugal extraction unit, a centrifugal back extraction unit, a nickel recycling feed liquid storage tank, an organic phase storage tank, a nickel recycling back liquid storage tank, a nickel recycling residual liquid storage tank, a back acid storage tank, an organic feed pump, a pipeline mixer, a heat exchanger and a saponification agent storage tank;
the outlet of the saponification agent storage tank and the discharge port of the organic phase storage tank are connected with the inlet of the organic feed pump through pipelines; the outlet of the organic feed pump is connected with the inlet of the pipeline mixer, and the outlet of the pipeline mixer is connected with the material inlet of the heat exchanger through a pipeline;
the material outlet of the heat exchanger is connected with the organic phase inlet of the first centrifugal extractor of the centrifugal extraction unit through a pipeline; the loaded organic phase outlet of the tail-stage centrifugal extractor of the centrifugal extraction unit is connected with the loaded organic phase inlet of the head-stage stripping centrifugal extractor of the centrifugal stripping unit through a pipeline; the organic phase outlet of the tail stage stripping centrifugal extractor of the centrifugal stripping unit is connected with the feed inlet of the organic phase storage tank through a pipeline;
the discharge port of the nickel recovery feed liquid storage tank is connected with the feed liquid inlet of the tail table centrifugal extractor of the centrifugal extraction unit through a pipeline; the raffinate outlet of the first centrifugal extractor of the centrifugal extraction unit is connected with the inlet of the nickel recovery raffinate storage tank through a pipeline;
the outlet of the acid reversing storage tank is connected with the acid inlet of the tail stage stripping centrifugal extractor of the centrifugal stripping unit through a pipeline; and a nickel-loaded reverse liquid outlet of the first stripping centrifugal extractor of the centrifugal reverse extraction unit is connected with an inlet of the nickel recovery reverse liquid storage tank through a pipeline.
2. The system for centrifugally extracting and recovering nickel from a solution containing low concentration nickel according to claim 1, wherein the centrifugal extraction unit comprises at least one centrifugal extractor, and when two or more centrifugal extractors are included, the loaded organic phase outlet of the former centrifugal extractor of the adjacent two centrifugal extractors is connected with the organic phase inlet of the latter centrifugal extractor through a pipeline; the raffinate outlet of the last centrifugal extractor of the two adjacent centrifugal extractors is connected with the feed liquid inlet of the previous centrifugal extractor through a pipeline.
3. The system for centrifugally extracting and recovering nickel from a solution containing low concentration nickel according to claim 1, wherein the centrifugal stripping unit comprises at least one stripping centrifugal extractor, and when two or more than two stripping centrifugal extractors are included, the loaded organic phase outlet of the former stripping centrifugal extractor of the adjacent two stripping centrifugal extractors is connected with the loaded organic phase inlet of the latter stripping centrifugal extractor through a pipeline; the nickel-loaded counter-liquid outlet of the back-extraction centrifugal extractor of the two adjacent counter-extraction centrifugal extractors is connected with the acid inlet of the front-extraction centrifugal extractor through a pipeline.
4. The system for centrifugally extracting and recycling nickel from a solution containing low concentration nickel according to claim 1, further comprising a backwashing unit, wherein a loaded organic phase outlet of a tail stage centrifugal extractor of the centrifugal extraction unit is connected with a loaded organic phase inlet of a head stage backwashing centrifugal extractor of the backwashing unit through a pipeline, and a loaded organic phase outlet of a tail stage backwashing centrifugal extractor of the backwashing unit is connected with a loaded organic phase inlet of a head stage stripping centrifugal extractor of the centrifugal stripping unit through a pipeline; the outlet of the acid-back storage tank is connected with the acid inlet of the back washing centrifugal extractor of the tail table of the back washing unit through a pipeline; and a backwash liquid outlet of the first backwash centrifugal extractor of the backwash unit is connected with a feed liquid inlet of the tail centrifugal extractor of the centrifugal extraction unit through a pipeline.
5. The system for centrifugally extracting and recovering nickel from a solution containing low concentration nickel according to claim 4, wherein the backwashing unit comprises at least one backwashing centrifugal extractor, and when two or more backwashing centrifugal extractors are included, the loaded organic phase outlet of the preceding backwashing centrifugal extractor of the adjacent two backwashing centrifugal extractors is connected with the loaded organic phase inlet of the following backwashing centrifugal extractor through a pipeline; the backwash liquid outlet of the back backwash centrifugal extractor of the two adjacent backwash centrifugal extractors is connected with the acid inlet of the front backwash centrifugal extractor through a pipeline.
6. The system for centrifugally extracting and recovering nickel from a solution containing low concentration nickel according to claim 1, further comprising a saponifier flowmeter, wherein an outlet of the saponifier reservoir is connected with an inlet of the saponifier flowmeter through a pipeline, and an outlet of the saponifier flowmeter and a discharge port of the organic phase reservoir are connected with an inlet of the organic feed pump through a pipeline; the saponifier flowmeter is a volumetric flowmeter.
7. The system for centrifugally extracting and recovering nickel from a solution containing low concentration nickel according to claim 1, further comprising a first acid counter-flow meter, wherein an outlet of the acid counter-flow tank is connected with an inlet of the first acid counter-flow meter through a pipeline, and an outlet of the first acid counter-flow meter is connected with an acid inlet of a final-stage stripping centrifugal extractor of the centrifugal stripping unit through a pipeline; the first counter acid flowmeter is a volumetric flowmeter.
8. The system for recovering nickel from a low concentration nickel containing solution according to claim 4, further comprising a second anti-acid flow meter, wherein the outlet of the anti-acid storage tank is connected with the inlet of the second anti-acid flow meter through a pipeline; the outlet of the second acid-back flowmeter is connected with the acid inlet of the back washing centrifugal extractor of the tail table of the back washing unit through a pipeline; the second acid counter flowmeter is a volumetric flowmeter.
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