NOVELTY - The process comprises performing physical preliminary operations, chemical extraction and recovery operations and treatment operations of the solutions to be recirculated in a cooperating relationship. The physical preliminary operations, chemical extraction and recovery operations and treatment operations comprise grinding and screening a fraction to the dimension of 1 mm to obtain a coarse fraction and a fine fraction, and performing a thermal treatment at temperatures of less than 400 degrees C for the paper and plastic combustion (or gravimetric separation).    USE - The process is useful for treating exhausted accumulators and batteries based on nickel/lithium.    ADVANTAGE - The process is capable of easily, effectively and economically treating the exhausted accumulators and batteries with high sensitivity and reduced energy consumption in an environmentally friendly manner.    DETAILED DESCRIPTION - The process comprises performing physical preliminary operations, chemical extraction and recovery operations and treatment operations of the solutions to be recirculated in a cooperating relationship. The physical preliminary operations, chemical extraction and recovery operations and treatment operations comprise grinding and screening a fraction to the dimension of 1 mm to obtain a coarse fraction and a fine fraction, performing a thermal treatment at temperatures of less than 400 degrees C for the paper and plastic combustion (or gravimetric separation) and then performing a densimetric separation of copper, separating aluminum before leaching using alkaline rinse and then recovering the aluminum in the form of alum, performing acidic-reducing leaching using hydrogen peroxide or a carbohydrate as the reducing agent from agri-food and paper industry wastes, where carbohydrate comprises monosaccharides, oligosaccharides and/or polysaccharides, primarily purifying the leach liquor using iron and aluminum hydroxides precipitation at pH of 5-5.5, separating cobalt from the leach liquor using a first extraction with an aprotic apolar organic solvent such as kerosene in the presence of a phosphinic acid derivative through a successive extraction and stripping cycles, obtaining a final aqueous phase rich in cobalt and intermediate aqueous phases from the first extraction, performing a second extraction in an apolar aprotic solvent in the presence of phosphinic acid by mixing final aqueous phase and intermediate aqueous phases together, and obtaining two different aqueous phases from the second extraction, where the one of the aqueous phases is rich in nickel and other of the aqueous phases is rich in manganese and/or lithium. The grinding and screening step is serially carried out on the coarse fraction of a magnetic separation of ferrous metals, and is preceded by a thermal pre-treatment at a temperature of 300-400 degrees C for 1 hour in nitrogen atmosphere. The step of obtaining the two different aqueous phases is carried out on their respective aqueous phases. The screening step is carried out by separating aluminum and copper from each other and crushing carried out on the fraction of less than 1 mm. The leaching operation is carried out by operating under stirring at a temperature of 70-90 degrees C and in acidic-reducing conditions with a ratio of sulfuric acid and fine of 2:1, and is preceded by a rinse phase at alkaline pH of 12.5-13 for 2 hours for the aluminum recovery, which is subsequently precipitated in the form of alum. The recovery of rare-earths is carried out by addition of alkali to a pH of 1-2 after leaching. The cobalt recovery by electrolysis is carried out in potentiostatic conditions with cathode potentials of 0.9-1.3 V, operating at pH of 4-4.5 at a room temperature and under moderate stirring using carbon steel or aluminum as the cathode and graphite or antimonium steel as the anode. The nickel recovery is carried out by working at cathode potentials of 0.9-1.3 V and operating at pH of 4-5 at the temperature of 30-40 degrees C on a nickel steel, copper or aluminum cathode. The lithium recovery is carried out by the solution coming from the manganese recovery, acidified to pH of 7-8 and then added with a saturated solution of sodium carbonate to pH of 8-9. A periodical crystallization of the currents coming from electrolysis reactors is carried out by evaporating 50 vol.% of water to be recirculated and subsequently cooling such a current to a temperature of 10-15 degrees C. The manganese recovery step is carried out before the cobalt separation using extraction with kerosene in the presence of a derivative of phosphoric acid through multiple extractive steps and a final stripping of all the organic phases. The manganese recovery is carried out in the form of a dioxide by precipitation at alkaline pH of 9 under an oxidizing atmosphere and then alternatively manganese recovery as a carbonate.    DESCRIPTION OF DRAWING(S) - The diagram shows a schematic view of a process for treating exhausted accumulators and batteries based on nickel/lithium.