TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Components: The first and second treatment agents of steps 3.1 and 3.2 are selected from hydroxides, carbonates, and/or bicarbonates of alkali metals. The hydroxides preferably are sodium hydroxide, potassium hydroxide, calcium hydroxide, lithium hydroxide; the carbonates preferably are sodium carbonate, potassium carbonate, calcium carbonate, or lithium carbonate; the bicarbonates preferably are sodium bicarbonate, potassium bicarbonate, lithium bicarbonate. The number of cycles is greater than 100.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Components: The number of cycles is greater than 3 (preferably greater than 15, especially greater than 30). The naphthalene sulfonic acid in the fusion mass is an H-acid. Preferred Method: For any single cycle the reaction sequence are carried out the stages of preparing separately diluted fusion mass and diluted acid, mixing together diluted fusion mass and diluted acid, where the stages are carried out in following stages: stage 1.1a of charging a first start up reaction medium to a first vessel with an agitator and charging to it an acid, preferably sulfuric acid, while maintaining the temperature of the acid up to 200 degrees C and pH of 1-7, where the quantity of first start up reaction medium is up to 40 (wt./wt.%) of the total amount of reaction medium used for this entire cycle, and the total amount of the first start up reaction medium used in the entire cycle is 5 to 100 (preferably 10-75) times, the total fusion mass to be isolated in the current cycle, stage 1.1b of charging a second start up reaction medium to a second reaction vessel with an agitator and charging to it fusion mass in a quantity such that the pH of the mixture in the second reaction vessel is 8-14 (preferably 9-13), where the quantity of second start up reaction medium is up to 40 (wt./wt.%) of the total amount of reaction medium used for this entire cycle, and the total amount of the second start up reaction medium used in the entire cycle is 5-100 (preferably 10-75) times the total fusion mass to be isolated in the current cycle, stage 1.1c of agitating mixtures of first and second reaction vessels for a duration up to 5 hours (preferably 30 minutes to 2.5 hours), while maintaining the temperatures of the respective mixtures at up to 200 degrees C, step 1.2 of charging the diluted fusion mass of the second reaction vessel to the diluted acid of the first reaction vessel over a period of up to 5 hours, and optionally charging a first reduction reaction medium and maintaining the temperature of the mixture to up to 200 degrees C and a pH of 1-9, where for all cycles beginning with the second cycle of the process, the first and second start up reaction mediums are drawn from a mother liquor storage tank where the mother liquor recycled from the recycle treatment sequence is stored, and the reaction mixture obtained at the end of step 1.2 is taken to a completion of the reaction sequence, followed by isolation of the product resulting from the reaction further followed by the recycle treatment of the mother liquor generated. For any single cycle the reaction sequence are carried out the stages of preparing separately diluted fusion mass and diluted acid, mixing together diluted fusion mass and diluted acid, where the stages are carried out in following steps: stage 1.1a of charging a first start up reaction medium to a first reaction vessel with an agitator and charging to it fusion mass in a quantity such that the pH of the mixture in the second reaction vessel is 8-14 (preferably 9-13), and the quantity of first start up reaction medium is up to 40 (wt./wt.%) of the total amount of reaction medium used for this entire cycle, and the total amount of the second start up reaction medium used in the entire cycle is 5-100 times (preferably 10-75 times) the total fusion mass to be isolated in the current cycle, stage 1.1b of charging a second start up reaction medium to a second vessel with an agitator and charging to it an acid, preferably sulfuric acid, while maintaining the temperature of the acid up to 200 degrees C and pH of 1-7, where the quantity of second start up reaction medium is up to 40 (wt./wt.%) of the total amount of reaction medium used for this entire cycle, and the total amount of the first start up reaction medium used in the entire cycle is 5-100 (preferably 10-75) times the total fusion mass to be isolated in the current cycle, stage 1.1c of agitating mixtures of first and second reaction vessels for a duration up to 5 hours, preferably 30 minutes-2.5 hours, while maintaining the temperatures of the respective mixtures at up to 200 degrees C, step 1.2 of charging the diluted acid of the second reaction vessel to the fusion mass of the first reaction vessel over a period of up to 5 hours, and optionally charging a first reduction reaction medium and maintaining the temperature of the mixture to up to 200 degrees C and a pH 1-9, where for all cycles beginning with the second cycle of the process, the first and second start up reaction mediums are drawn from a mother liquor storage tank where the mother liquor recycled from the recycle treatment sequence is stored, and the reaction mixture obtained at the end of step 1.2 is taken to a completion of the reaction sequence, followed by isolation of the product resulting from the reaction further followed by the recycle treatment of the mother liquor generated. For any cycle of the process the reaction mixture obtained at the end of the step 1.2 is taken to completion of reaction sequence as follows: step 1.3 of optionally adding to the first reaction vessel a second reaction medium in a quantity up to 40 (wt./wt.%) of the total amount of reaction medium used for this entire cycle while optionally stirring the mixture at up to 500 RPM and by maintaining the temperature of the reaction mixture at up to 200 degrees C (preferably up to 100 degrees C), and carrying out the stirring for up to 10 hours (preferably 30 minutes to 8 hours) so that complete removal of sulfur dioxide generated during the reaction takes place, and the Baume value is 10 to 50, step 1.4 of adding in the first cycle a third reaction medium in the form of fresh reaction medium to the first reaction vessel in a quantity not exceeding 40 (wt./wt.%) of the total amount of reaction medium used in the entire current cycle to form a separation mixture, while maintaining the temperature of the separation mixture up to 200 degrees C, preferably up to 100 degrees C, and the pH of 1-7 while stirring the separation mixture for up to 24 hours, preferably up to 5 hours, where the third reaction medium used for all following cycles is selected from the mother liquor storage tank. For any cycle of the process the isolation sequence comprises the following steps: step 2.1 of a first stirring reaction medium in the form of a fresh reaction medium is charged to the first reaction vessel in a quantity not exceeding 60 (wt./wt.%) of the total quantity of reaction medium used in the current cycle, while allowing the mixture to cool to a temperature of 70 degrees C, and by maintaining its pH of 1-7, while continuously stirring the mixture for up to 10 hours, where for all following cycles the first stirring reaction medium is taken from the mother liquor storage tank, step 2.2 of maintaining the temperature of the reaction mixture at 70 degrees C and pH at 1 to 7 by optionally adding a fourth reaction medium in the form of a fresh reaction medium in the first cycle, while stirring the reaction mixture for a duration of up to 24 hours, preferably up to 5 hours, where for all following cycles the first stirring reaction medium is taken from the mother liquor storage tank, step 2.3 of filtering the separation mass formed at the end of step 2.2 at a temperature of about 70 degrees C and pH at 1 to 7, and generating a first filtrate stream A as a result of the filtration process, the process of filtration taking place over a period of up to 5 hours, step 2.4 of washing the total mass obtained at the end of step 2.3 using fresh reaction medium at a temperature of 70 degrees C and a pH of 1 to 7, and generating the washing stream B. For any cycle of the process the first filtrate stream A and the washing stream B and combined and subjected to a catalytic treatment as follows: step 3.1 of heating in a first treatment vessel the combined streams A and B to a temperature up to 100 degrees C, preferably 70 degrees C, for up to 5 hours, followed by adding a first treatment agent and a first sulfate salt, where the quantity of the first treatment agent is up to 40 (wt./vol.%) of the total quantity of the reaction medium used in the current cycle, such that the Baume value of the mixture is maintained at up to 50 while maintaining the temperature of the mixture after addition of the agent maintained at up to 50 degrees C, and pH at 1-7, so that a second filtrate in the form of mother liquor stream C is generated as well as spent material which needs disposing of fresh sulfate salt is used only in the first cycle of this step and in the following cycles, the salt generated from step 3.2 is used, step 3.2 of charging the second filtrate stream C to a second treatment vessel where the second filtrate is cooled to a temperature of up to 25 degrees C for up to 5 hours followed by charging of a second treatment agent and sulfate salt, where the second treatment agent and sulfate salt is in a quantity up to 20 (wt./vol.%) of the total quantity of reaction medium used in the current cycle, while maintaining the Baume value of the mixture up to 50, and the pH 1 to 7, preferably 4 to 6, where in the first cycle of the process, fresh salt is used and in all following cycles the salt recovered at the end of step 3.2 is used. The acid is sulfuric acid. The first and second treatment agents are any proprietary agents. The fusion mass and/or acid is added to the step 1.2 in its entire quantity or in batches of any size at any interval. The first and second treatment agents are either added together in small lots till the temperature of the reaction mixture reaches 0-100 degrees C (preferably 70 to 20 degrees C), or alternatively both agents are added together once the temperature has reached 0-100 degrees C (preferably 70 to 20 degrees C). EXAMPLE - No suitable example given.