A treatment method of a chlorine-containing zinc oxide secondary material, wherein, the method comprises the following steps: Leaching the chlorine-containing zinc oxide secondary material I through an acid solution to obtain leaching liquor and leaching residue; Selectively extracting zinc from leaching liquor obtained from the Step through P 204- kerosene solvent to obtain a zinc-containing organic phase as well as chlorine and acid containing raffinate; Implementing stripping-electrolysis zinc recovery to the zinc-containing organic phase obtained from the Step, and returning the organic phase after the stripping to the Step to extract zinc; Taking the raffinate obtained from the Step as the acid solution of the Step, returning to Step and repeating -; Taking out the raffinate obtained from the Step, when the chlorine ion of chlorine-containing aqueous phase in the step achieves 50-80g/L after circulating repeating steps -, wherein the number of taking out the raffinate shall guarantee the chlorine content of the taken out raffinate is identical to that of raw material added in the Step so as to keep chlorine ion adding and taking out balance; mixing the taken out raffinate with additional chlorine-containing zinc oxide secondary material II at liquid-solid ratio of 1-3: 1; carrying out liquid-solid separation; leaching the separated deposit through acid raffinate of the Step; Removing impurities of chlorine-containing aqueous phase to obtain the solution containing KCl and NaClwhen the Step is completedand the separated solution contains 80-120g/L of chlorine ion and 160-240g/L of total salt content; Evaporating and concentrating the KCl and NaCl mixing solution obtained from the Step to crystallize out KCl and NaCl products. Leaching the chlorine-containing zinc oxide secondary material I through an acid solution to obtain leaching liquor and leaching residue; Selectively extracting zinc from leaching liquor obtained from the Step through P 204- kerosene solvent to obtain a zinc-containing organic phase as well as chlorine and acid containing raffinate; Implementing stripping-electrolysis zinc recovery to the zinc-containing organic phase obtained from the Step, and returning the organic phase after the stripping to the Step to extract zinc; Taking the raffinate obtained from the Step as the acid solution of the Step, returning to Step and repeating -; Taking out the raffinate obtained from the Step, when the chlorine ion of chlorine-containing aqueous phase in the step achieves 50-80g/L after circulating repeating steps -, wherein the number of taking out the raffinate shall guarantee the chlorine content of the taken out raffinate is identical to that of raw material added in the Step so as to keep chlorine ion adding and taking out balance; mixing the taken out raffinate with additional chlorine-containing zinc oxide secondary material II at liquid-solid ratio of 1-3: 1; carrying out liquid-solid separation; leaching the separated deposit through acid raffinate of the Step; Removing impurities of chlorine-containing aqueous phase to obtain the solution containing KCl and NaClwhen the Step is completedand the separated solution contains 80-120g/L of chlorine ion and 160-240g/L of total salt content; Evaporating and concentrating the KCl and NaCl mixing solution obtained from the Step to crystallize out KCl and NaCl products.