7  5,648,520  8  The distillate  (X),  which is contaminated  with hydropho› bic solvent and  auxiliary amine,  is most suitable  for the  washing stages  (7.0)  and  (8.0).  The resulting washing  waters  generally exhibit  a very much lower  acid  concentration  than  the actual acid circulation,  such that they are  able to be  It has proved to be  expedient to liberate  the organic phases  (D) and (D’) and  (L) and (L’),  respectively, which  are  This latter also includes  the washing stages  (7.0)  and/or  (8.0).  The latter are extraction  stages acting in  single or  multi-stage manner  operating on the  countercurrent  prin› ciple. In washing  stage  (7.0)  the organic phase  (D) or (D’) is  liberated from adhering  traces of acid with  a partial stream  of  (X),  and in the washing  stage  (8.0)  the same is effected  with the organic  phase  (L)  or  (L’)  using another partial  stream of  (X).  The recovery of  hydrophobic solvent  and of auxiliary  amine is generally  associated with an  extensive, optionally  complete separation  of the two  components,  and affords, on  the one hand, in the  form of distillate  streams  (E)  and  (M),  hydrophobic solvent  which is to a large  extent impoverished  at least as to auxiliary  amine, optionally  to a large extent  liberated from auxiliary  amine, and affords  auxiliary amine  which is to a large  extent impoverished  at least as to  hydrophobic solvent,  optionally to  a large extent liberated  from hydrophobic  solvent, in the form  of distillate streams  (F)  and  (N),  generally united in  stream (S).  The water volume  (X)  which is removed  is, optionally  after being split  into partial streams  and after being used  variously, supplied  again to the system  at a suitable point  in  the form of the stream  (Y)  in its entirety or in  partial streams,  such that there results  an enlarged and optionally  branched  closed-circuit aqueous  system.  The working-up  stages  (7)  and  (8)  serve to separate  the  polyamine fractions  which arise as distillation  residues and  are isolated as process  products (G) and (0)  in the tanks  (10)  and  (11),  and to recover as  distillates the hydrophobic  solvent utilized and  the auxiliary amine  used.  The extraction stages  (5)  and  (6)  are generally embodied  as extractors acting  in  multi-stage manner.  The extraction stage  (4)  is in the simplest  case a mixer› settler unit acting  in single stage manner,  however extraction  units acting in multi-stage  manner are preferably  used.  In the aqueous phase,  which contains the  acid, there is  present in practical  terms a closed circuit  such that the stage  (9)  can be inserted  fundamentally  at any point in the  latter  circulation system.  The position of stage  (9)  following the  extraction stage  (  6)  and before entry into  the extraction stage  (2), (3)  or  (4)  is the most  advantageous  and hence the  preferred embodiment.  Such a step is  fundamentally  not a necessity for  carrying  out the process according  to the invention, however  because  of the  advantages those  embodiments which  include a water  distillation stage  (9)  are preferred.  The extraction stage  (3)  which is optionally  interposed  likewise also comprises  in the simplest instance  a mixer› settler unit, however  here too extraction  units acting in  multi-stage manner  are preferably used.  The extraction stage  (2)  positioned upstream  is generally  embodied as an extractor  acting in multi-stage  manner.  Reference letters  A-Z  designate the streams  to which  reference is made  hereinbelow  and in the Examples.  The distillation stage  (9)  is an apparatus with  which water  can be removed by  distillation from the  aqueous phase of  the  system or from a  partial stream of  the aqueous phase.  The extensive, optionally  complete, separation  by distil› lation of hydrophobic  solvent and auxiliary  amine is pre› ferred in carrying  out the process according  to the invention,  and this applies in  particular to the  distillate fractions  (M)  and  (E).  The working-up  stage  (8)  also generally composes  an at  least two-stage multi-stage  distillation whereof  the first stage  (8.1)  delivers as the distillate  (M)  a  hydrophobic solvent  liberated, by comparison  with the intake product  (L) or  (L’),  from polyamine  and  impoverished  as to auxiliary amine,  optionally liberated  from auxiliary amine,  and whereof the  final stage  (8.2)  delivers as the distillate  (N)  an auxiliary  amine which, by  comparison with  (L)  or (L’), is liberated  from  polyarylamine  and  impoverished  as to  hydrophobic  solvent, optionally  liberated from hydrophobic  solvent.  Additionally there  arises in the final  distillation stage  (7.2),  as the distillate  bottoms (G), the  first polyamine  fraction of the starting  mixture (A), which  was contained in  stream (D) or (D’).  The actual working-up  stage  (7)  generally comprises  an at  least two-stage multi-stage  distillation whereof  the first stage  (7.1)  delivers as the distillate  (E) a  hydrophobic solvent  which by comparison  with the intake product  (D) or (D’) is  liberated from polyarylamine  and is  impoverished  as to  auxiliary amine,  optionally liberated  from auxiliary amine,  and whereof the final  stage  (7 .2)  delivers as the distillate  (F)  an auxiliary amine  which by comparison  with (D) or (D’) is  liberated from polyarylamine  and  impoverished  as to hydro› phobic solvent, optionally  liberated from hydrophobic  sol- vent.  supplied to the distillation  stages, from adhering  traces of  acid, by extracting  with water, before  their treatment by  distillation  in the washing stages  (7.0)  and  (8.0)  positioned  upstream.  Primary  anilines are preferably  used, with aniline  particu› larly preferred.  The process according  to the invention may  be carried out  both batchwise and  continuously.  A preferred  embodiment  is  the continuous mode,  in which the process  is carried out in  all stages under  the pressure inherent  in the system and  preferably in an inert  gas atmosphere (nitrogen).  The process according  to the invention may  be repeated  with each of the product  fractions arising in  order to increase  the enrichment or  corresponding impoverishment  effect  The process according  to the invention may  be carried out  both with three (FIG.  1)  and also with four  (FIGS.  2  and  3)  or five extraction  stages (FIG.  4).  The flow diagrams  of FIGS.  1-4  serve to explain further  the process according  to the invention,  with the following  references:  (1)  a tank for the starting  arylamine mixture  (2)  an extraction stage  (positioned upstream)  (3)  an extraction stage  (interposed)  (4)  a (first)  extraction stage  (5)  a  (penultimate) extraction  stage  (6)  a (final)  extraction stage  (7)  a  working-up stage  comprising  (7.0)  a washing stage,  (7.1)  a first  distillation stage  of a  multi-stage distillation,  (7.2)  a final  distillation stage of  a  multi-stage distillation,  (8)  a further  working-up stage  comprising  (8.0)  a washing stage,  (8.1)  a first  distillation stage  of a further  multi-stage  distillation,  (8.2)  a final  distillation stage  of a further  multi-stage  distillation,  (10)  a tank for a process  product  (9)  a water  evaporator  (11)  a  tank  for a further process  product. 