below embodiments and / or example of the present disclosure are further described . drinking water was processed using conventional techniques and then processed using ion exchange resins to perform deep purification of water . as illustrated in fig1 , the ion exchange resins may be regenerated after treatment of a certain amount of water . at normal temperature and pressure , the ion exchange resins were regenerated using a regeneration solution containing 35 % nacl for about 30 minutes . after the regeneration , the regeneration solution became a desorption solution in which the concentration of toc is about 2116 mg / l and an amount of nacl is about 16 . 8 %. the desorption solution was placed in a coagulation tank , was added polyaluminium chloride ( pac ) 1000 mg / l for stirred coagulation , and was left for settlement for about 2 hours . sludge at the bottom of the coagulation tank was filtered using a pressure filter and a volume of the dry sludge is about 1 . 0 %. the pressure sludge filtrate and the coagulation serum were placed into a tank for the regeneration solution . a removal rate of toc using the coagulation is about 41 %, a concentration of toc in the pressure sludge filtrate and the coagulation serum is about 1250 mg / l and an amount of nacl is about 16 . 8 %. a certain amount of nacl regeneration solution was added to the tank for the regeneration solution such that the amount of nacl is about 33 % and the concentration of toc is still about 1250 mg / l in the newly made regeneration solution . the regeneration solution was then placed into the ion exchange resins to resin regeneration . accordingly , the newly produced desorption solution generated by coagulation was added nacl regeneration solution to regenerate the ion exchange resins for three batches . the desorption solution desorbed organic contents from the ion exchange resins , and toc values of the organic contents were 1830 mg / l , 1518 mg / l , and 1208 mg / l , respectively . after three batches , the regeneration rate of the regeneration solution was less than 60 % and the current regeneration solution was capable of desorbing organic contents having a toc value of 1208 mg / l . the desorption solution was then drained away . at this point , the amount of the desorption solution was reduced to ¼ of those produced by conventional techniques . operating conditions of example 2 is similar to those of example 1 . the desorption solution was placed in a coagulation tank and was added pac to reach 3000 mg / l of pac . after coagulation , a toc removal rate of the desorption solution is about 52 %. after coagulation of the desorption solution , the regeneration solution was made and four batches were applied . the desorption solution desorbed organic contents from the ion exchange resins , and toc values of the organic contents were 2120 mg / l , 1918 mg / l , 1695 mg / l , 1456 mg / l , and 1210 mg / l , respectively . after four batches , the regeneration rate of the regeneration solution was less than 60 % and the desorption solution was then drained away . at this point , the amount of the desorption solution was reduced to ⅕ of those produced by conventional techniques . operating conditions of example 3 is similar to those of example 1 . the desorption solution was placed in a coagulation tank and was added polymeric ferric chloride to have a concentration of 1000 mg / l of polymeric ferric chloride . after coagulation , a toc removal rate of the desorption solution is about 62 %. after coagulation of the desorption solution , the regeneration solution was made and five batches were applied . the desorption solution desorbed organic contents from the ion exchange resins , and toc values of the organic contents were 2118 mg / l , 1940 mg / l , 1788 mg / l , 1590 mg / l , 1478 mg / l , and 1245 mg / l , respectively . after five batches , the regeneration rate of the regeneration solution was less than 60 % and the desorption solution was then drained away . at this point , the amount of the desorption solution was reduced to ⅙ of those produced by conventional techniques . operating conditions of example 4 is similar to those of example 3 . the desorption solution was placed in a coagulation tank and was added polymeric ferric chloride 3000 mg / l . after coagulation , a toc removal rate of the desorption solution is about 76 %. after coagulation of the desorption solution , the regeneration solution was made and seven batches were applied . the desorption solution desorbed organic contents from the ion exchange resins , and toc values of the organic contents were 2125 mg / l , 2018 mg / l , 1902 mg / l , 1785 mg / l , 1656 mg / l , 1538 mg / l , 1390 mg / l , 1235 mg / l , respectively . after seven batches , the regeneration rate of the regeneration solution was less than 60 % and the desorption solution was then drained away . at this point , the amount of the desorption solution was reduced to ⅛ of those produced by conventional techniques . drinking water was processed using conventional techniques and then processed using ion exchange resins to perform deep purification . at normal temperature and pressure , the ion exchange resins were regenerated using a regeneration solution containing 35 % nacl for about 30 minutes . after the regeneration , the regeneration solution became a desorption solution in which the concentration of codcr is about 7218 mg / l and an amount of nacl is about 14 . 6 %. the desorption solution was placed in a coagulation tank , was added pac to have a concentration of 1000 mg / l of pac for stirred coagulation , and was left to settle for about 2 hours . sludge at the bottom of the coagulation tank was filtered using a pressure filter and a volume of the dry sludge is about 1 . 5 %. the pressure sludge filtrate and the coagulation serum were placed into a tank for the regeneration solution . a removal rate of codcr using the coagulation is about 42 %, a concentration of codcr in the pressure sludge filtrate and the coagulation serum is about 4186 mg / l and an amount of nacl is about 14 . 6 %. a certain amount of nacl regeneration solution was added to the tank for the regeneration solution such that the amount of nacl is about 33 % and the concentration of codcr is still about 4186 mg / l in the newly made regeneration solution . the regeneration solution was then placed into the ion exchange resins to resin regeneration . accordingly , the newly produced desorption solution generated by coagulation was added nacl regeneration solution . the ion exchange resins were regenerated and two batches were applied . the desorption solution desorbed organic contents from the ion exchange resins , and codcr values of the organic contents were 5930 mg / l and 4335 mg / l . after two batches , the regeneration rate of the regeneration solution was less than 60 % and the current regeneration solution was capable of desorbing organic contents having a codcr value of 4335 mg / l . the desorption solution was then drained away . at this point , the amount of the desorption solution was reduced to ⅓ of those produced by conventional techniques . operating conditions of example 6 is similar to those of example 5 . the desorption solution was placed in a coagulation tank and was added pac to have a concentration of 3000 mg / l of pac . after coagulation , a codcr removal rate of the desorption solution is about 53 %. after coagulation of the desorption solution , the regeneration solution was made and three batches were applied . the desorption solution desorbed organic contents from the ion exchange resins , and codcr values of the organic contents were 7230 mg / l , 6520 mg / l , 5542 mg / l , and 4360 mg / l , respectively . after three batches , the regeneration rate of the regeneration solution was less than 60 % and the desorption solution was then drained away . at this point , the amount of the desorption solution was reduced to ¼ of those produced by conventional techniques . operating conditions of example 7 is similar to those of example 5 . the desorption solution was placed in a coagulation tank and was added polymeric ferric chloride to have a concentration of 1000 mg / l of polymeric ferric chloride . after coagulation , a codcr removal rate of the desorption solution is about 61 %. after coagulation of the desorption solution , the regeneration solution was made and four batches were applied . the desorption solution desorbed organic contents from the ion exchange resins , and codcr values of the organic contents were 7220 mg / l , 6721 mg / l , 6070 mg / l , 5290 mg / l , and 4338 mg / l , respectively . after four batches , the regeneration rate of the regeneration solution was less than 60 % and the desorption solution was then drained away . at this point , the amount of the desorption solution was reduced to ⅕ of those produced by conventional techniques . operating conditions of example 8 is similar to those of example 7 . the desorption solution was placed in a coagulation tank and was added polymeric ferric chloride 3000 mg / l . after coagulation , a codcr removal rate of the desorption solution is about 75 %. after coagulation of the desorption solution , the regeneration solution was made and five batches were applied . the desorption solution desorbed organic contents from the ion exchange resins , and toc values of the organic contents were 7216 mg / l , 6805 mg / l , 6366 mg / l , 5720 mg / l , 5080 mg / l , 4315 mg / l , respectively . after five batches , the regeneration rate of the regeneration solution was less than 60 % and the desorption solution was then drained away . at this point , the amount of the desorption solution was reduced to ⅙ of those produced by conventional techniques . wastewater was processed using conventional techniques and then processed using ion exchange resins to perform deep purification . as illustrated in fig1 , the ion exchange resins may be regenerated after treatment of a certain amount of water . ( a ) at normal temperature and pressure , the ion exchange resins were regenerated by mixing ion exchange resins to be generated and a regeneration solution containing 35 % nacl for about 10 minutes . the ion exchange resins were regenerated and the regeneration solution became the desorption solution . ( b ) adding a coagulant to the desorption solution to perform coagulating sedimentation . the desorption solution was added polymeric ferric chloride to have a concentration of 100 mg / l of polymeric ferric chloride . ( c ) performing a slurry separation on the desorption solution after the coagulating sedimentation to form a coagulation serum and generate an amount of sludge that is disposed . a ratio between a volume of the coagulation serum and a volume of the desorption solution is about 99 . 5 %. ( d ) adding an amount of a regeneration agent to the coagulation serum to form the regeneration solution . the regeneration agent is potassium chloride and the amount of the added regeneration agent is about 5 % of an amount of the regeneration solution . ( e ) performing operations of the step ( a ) using the regeneration solution formed in the step ( d ) to regenerate the ion exchange resins . ( f ) repeating two batches of the steps ( a ) to ( e ). in response to a determination that the regeneration solution fails to satisfy a predetermined condition , disposing the desorption solution . operating conditions of example 10 is similar to those of example 9 . at step ( a ), at normal temperature and pressure , the ion exchange resins were regenerated by mixing ion exchange resins to be generated and a regeneration solution containing 36 % sodium bicarbonate for about 60 minutes . at step ( b ), the desorption solution was added aluminum sulfate to have a concentration of 2000 mg / l of aluminum sulfate . in step ( c ), a ratio between a volume of the coagulation serum and a volume of the desorption solution is about 93 %. at step ( d ), the amount of the added regeneration agent is about 30 % of an amount of the regeneration solution . the number of multiple batches is 8 . operating conditions of example 11 is similar to those of example 9 . at step ( a ), at normal temperature and pressure , the ion exchange resins were regenerated by mixing ion exchange resins to be generated and a regeneration solution containing potassium hydroxide for about 120 minutes . at step ( b ), the desorption solution was added pac to have a concentration of 5000 mg / l of pac . in step ( c ), a ratio between a volume of the coagulation serum and a volume of the desorption solution is about 80 %. at step ( d ), the amount of the added regeneration agent is about 40 % of an amount of the regeneration solution . the number of multiple batches is 30 . operating conditions of example 12 is similar to those of example 9 . at step ( a ), at normal temperature and pressure , the ion exchange resins were regenerated by mixing ion exchange resins to be generated and a regeneration solution containing sodium hydroxide for about 100 minutes . at step ( b ), the desorption solution was added polyacrylamide to have a concentration of 100 mg / l of polyacrylamide . in step ( c ), a ratio between a volume of the coagulation serum and a volume of the desorption solution is about 86 %. at step ( d ), the amount of the added regeneration agent is about 5 % of an amount of the regeneration solution . the number of multiple batches is 13 . operating conditions of example 13 is similar to those of example 9 . at step ( a ), at normal temperature and pressure , the ion exchange resins were regenerated by mixing ion exchange resins to be generated and a regeneration solution containing a mixture of sodium chloride , potassium chloride , sodium bicarbonate , sodium hydroxide and potassium hydroxide for about 110 minutes . a mass ratio of sodium chloride , potassium chloride , sodium bicarbonate , sodium hydroxide and potassium hydroxide in the mixture is 5 : 5 : 5 : 5 : 1 , respectively . at step ( b ), the desorption solution was added a mixture of pac , aluminum sulfate , ferric chloride polymerization , pfs and polyacrylamide to have a concentration of 4000 mg / l of the mixture . a mass ratio of pac , aluminum sulfate , ferric chloride polymerization , pfs and polyacrylamide in the mixture is 10 : 10 : 10 : 10 : 1 , respectively . in step ( c ), a ratio between a volume of the coagulation serum and a volume of the desorption solution is about 91 %. at step ( d ), the amount of the added regeneration agent is about 15 % of an amount of the regeneration solution . the number of multiple batches is 9 . operating conditions of example 12 is similar to those of example 9 . at step ( a ), at normal temperature and pressure , the ion exchange resins were regenerated by mixing ion exchange resins to be generated and a regeneration solution containing a mixture of sodium chloride , sodium bicarbonate , and sodium hydroxide for about 75 minutes . a mass ratio of sodium chloride , sodium bicarbonate , and sodium hydroxide in the mixture is 10 : 5 : 1 , respectively . at step ( b ), the desorption solution was added a mixture of ferric chloride polymerization , pac , and polypropylene amide to have a concentration of 2800 mg / l of the mixture . a mass ratio of ferric chloride polymerization , pac , and polypropylene amide in the mixture is 20 : 5 : 1 , respectively . in step ( c ), a ratio between a volume of the coagulation serum and a volume of the desorption solution is about 87 %. at step ( d ), the amount of the added regeneration agent is about 10 % of an amount of the regeneration solution . the number of multiple batches is 15 .