Aug. 19, 2010  12  US 2010/0210871 Al  isobutyl methyl ketone.  An  ion chromatography analysis of  the organic phase showed an ammonium content of <l 00  ppm.  [0137]  Extraction ofMHA from a 10% MHA ammonium  salt solution with isobutyl methyl ketone in a countercurrent  extractor (inventive) 43 .3 g (239 mmol, M= 167 .2 g/mol, with  a content of92.3%) ofMHA ammonium salt were dissolved  in 356.7 g of water. This 10% salt solution was initially  charged in the reservoir vessel of the countercurrent extractor  (FIG.  2)  and heated to 80°  C. 1333 g ofisobutylmethylketone  were likewise heated to 80°  C. in the solvent reservoir. The  extractor colunm was filled at the start with aqueous salt  solution. During the extraction, 60 1 of nitrogen per hour were  allowed to bubble continuously through the liquid colunm.  Both liquid circulations were kept constant over the total  extraction time. The aqueous salt solution was pumped in  circulation at 5 ml/min and the isobutyl methyl ketone at 8  ml/min. The effluxing MBA-containing isobutyl methyl  ketone phase was passed into the distillation vessel via the  heated phase separator (80°  C.). The isobutyl methyl ketone  which was distilled off under gentle conditions was fed back  into the circuit via the solvent reservoir. The MHA extracted  remained in the distillation flask with isobutyl methyl ketone  which had not been distilled off. After 90 hours, the extraction  was ended and the yellow-coloured isobutyl methyl ketone  from the distillation and the aqueous phase were weighed and  analysed by HPLC. 4% of the MHA used was still found in  the aqueous phase, 95% in the isobutyl methyl ketone.  An  ion  chromatography analysis of the organic phase showed an  ammonium content of <l 00 ppm.  [0138]  Extraction of (+)-camphor-I 0-sulphonic acid from  a 10% (+)-camphor-I 0-sulphonic acid ammonium salt solu› tion with isobutyl methyl ketone in a specific rotational per› forator using an entraining gas as the stripping medium (in› ventive) 21.3 g (90 mmol, M=232.30 g/mol, with a content of  98%) of (+)-camphor-I 0-sulphonic acid were initially  charged in 50 g of water and admixed with 6.5 ml of 32%  aqueous ammonia solution (0.1 mo!). After stirring for 30  minutes, the excess ammonia and most of the water were  drawn off from the clear colourless solution at 40°  C. in a  water-jet vacuum. The resulting white solid (39.8 g) was  dissolved in 209.5 g of water. This 10% salt solution was  initially charged in the rotational perforator (FIG.  1)  and  heated to 80°  C. The solvent flask was initially charged with  500 g of isobutyl methyl ketone which were heated to boiling  (internal temperature 115-117°  C.). 6 1 of nitrogen per hour  were passed continuously through the aqueous salt solution.  After 66 hours, the extraction was ended and the pale-co› loured isobutyl methyl ketone and the aqueous phase were  concentrated to dryness. 74% of the (+)-camphor-10-sul› phonic acid used was still found in the aqueous phase, 25% in  the isobutyl methyl ketone.  An  ion chromatography analysis  of the organic phase showed an ammonium content of <l 00  ppm.  [0139]  Extraction oftoluenephosphonic acid from a 10%  toluenephosphonic acid ammonium salt solution with isobu› tyl methyl ketone in a specific rotational perforator using an  entraining gas as the stripping medium (inventive) 20.0 g  (113.9 mmol, M=l 72.12 g/mol, with a content of 98%) of  toluenephosphonic acid were initially charged in 50 g of  water and admixed with 8.5 ml of 32% aqueous ammonia  solution (0.13 mo!). After stirring for 30 minutes, the excess  ammonia and most of the water were drawn off from the clear  colourless solution at 40°  C. in a water jet vacuum. The  resulting oil (24.5 g) was dissolved in 190.9 g of water. This  10% salt solution was initially charged in the rotational per› forator (FIG.  1)  and heated to 80°  C. The solvent flask was  initially charged with 500 g of isobutyl methyl ketone which  were heated to boiling (internal temperature 115-117°  C.). 6  1 of nitrogen per hour were passed continuously through the  aqueous salt solution. After 23 hours, the extraction was  ended and the pale-coloured isobutyl methyl ketone and the  aqueous phase were concentrated to dryness. 56% of the  toluenephosphonic acid used was still found in the aqueous  phase, 43% in the isobutyl methyl ketone.  An  ion chromatog› raphy analysis of the organic phase showed an ammonium  content of <l 00 ppm.  1-19.  (canceled)  20.  A process for converting an ammonium salt of an  organic acid to a free organic acid, comprising:  a) contacting an aqueous solution of the ammonium salt  with an organic extractant;  b) dissociating said ammonium salt at a temperature and  pressure at which the aqueous solution and the extract› ant are in a liquid state; and  c) introducing a stripping medium or entraining gas in  order to remove NH$_{3 }$ from the aqueous solution and  transfer at least a portion of the free organic acid formed  to the organic extractant.  21.  The process of claim  20,  wherein the conversion is  carried out at a pressure of 0.01 bar to 20 bar.  22.  The process of claim  21,  wherein the salt dissociation is  performed at a temperature of 20°  C. to 300°  C.  23.  The process of claim  20,  wherein:  a) the conversion is carried out at a pressure of0.01 bar to  200 bar;  b) salt dissociation is performed at a temperature of 5°  C. to  300°  C.; and  c) the starting concentration of the ammonium salt of an  organic acid in the aqueous solution used is in the range  of from 90% by weight to 1 % by weight.  a) the conversion is carried out at a pressure of0.1 bar to 5  bar;  b) salt dissociation is performed at a temperature of 50°  C.  to 130°  C.;  c) the starting concentration of the ammonium salt of an  organic acid in the aqueous solution used is in the range  of from 60% by weight to 10% by weight;  24.  The process of claim  23,  wherein the extractant used is  a sparingly water-miscible or entirely water-immiscible sol› vent.  25.  The process of claim  24,  wherein the weight ratio of  aqueous solution to organic extractant is from 1: 100 to 100: 1.  26.  The process 20, wherein the organic acid is selected  from the group consisting of: monocarboxylic acid; dicar› boxylic acid; tricarboxylic acid; ascorbic acid;  27.  The process of claim  26,  wherein,  sulphonic acid; phosphonic acid; and hydroxycarboxylic  acid.  Example 10  Example 12  Example 13 