the chemical reactions occurring in an electrolytic cell according to this invention are represented by the following equations : ## str1 ## because of the cationic membrane separating the electrode compartments , sodium hydroxide formed at the cathode cannot enter the anode compartment and increase the alkalinity of the anolyte . because of this feature , the process of the present invention does not require neutralization of the anolyte which was necessary in the process of the above - discussed u . s . pat . no . 2 , 385 , 410 . another problem which plagued prior attempts was product build - up on the anode . it has now been unexpectedly discovered that shiny platinum is the only active anode material which is not subject to product build - up , especially if the anolyte is agitated . it is not necessary that the entire anode be made of shining platinum , such as foil or wire , but it can also be made by rolling a layer of platinum on a suitable substrate , such as , for example , titanium , tantalum , and columbium . these metals are passive in contact with the anolyte and will not cause product accumulation . the cathode may be made of any suitable material . the most commonly used cathode material is mild steel . other possible materials include , for example , stainless steel and titanium . while precious metals such as platinum , gold , iridium , or palladium , also are suitable cathode materials , their high cost makes them impractical for this application . with presently available cationic membranes , the sodium hydroxide concentration in the cathode compartment preferably should not be higher than 17 weight percent . above this concentration , the cationic membrane would lose selectivity sufficiently and would allow hydroxyl ions into the anode compartment in amounts which would alter the ph and bring about the formation of undesirable by - products . however , as membranes which still are selective at high caustic concentrations become available , such higher concentrated caustic can be used . the catholyte is continuously diluted by water because each na + ion going through the cationic membrane is accompanied by about twelve water molecules . the number of molecules of water that pass through the membrane for each na + ion depends on the membrane used . additional water may be added , if desired , directly to the catholyte continuously or intermittently . excess catholyte usually will be drained . while under the preferred conditions the anolyte temperature is at least 60 ° c ., the catholyte temperature may be lower or higer . usually , there will be a difference of a few degrees between the electrolytes in both compartments . the discovery that shiny platinum is the only suitable active anode surface material is surprising because other metals can be obtained in the same degree of surface smoothness and are as inert chemically , yet are unsuitable . these include , for example , gold , nickel and stainless steel . it is not certain whether material build - up encountered with such materials in prior art processes is due to the fact that impure , sticky product is formed which tends to adhere to the anode surface ; or , conversely , the product which builds up on the anode is eventually decomposed in part and thus is of inferior quality . the product obtained by the process of the present invention is , however , white and has a high melting point ; it is a high purity material . while the present disclosure is mainly concerned with the electrolysis of sodium dialkyldithiocarbamates , other dialkyldithiocarbamate salts can be used in this process . these would be especially potassium and lithium salts but may also be other alkali metal , ammonium , and quaternary ammonium salts . the cationic membrane required in the process of the present invention can be any commercially available , organic or inorganic membrane , such as , for example , a nafion ® cationic membrane available from e . i . du pont de nemours and company , wilmington , delaware . the preferred dialkyldithiocarbamate concentration in the anode compartment provides maximum current efficiency . a 30 % solution has the highest conductivity . the conductivity of solutions more dilute than 20 % may be too low for practical operation ; above 40 %, a slurry is formed and the conductivity is quite low . in addition , outside the preferred concentration limits danger of overoxidation arises . the desired current efficiency is at least about 90 %. the &# 34 ; inefficient &# 34 ; current may produce either innocuous products such as hydrogen and oxygen from electrolytic decomposition of water or tetraalkylthiuram disulfide degradation products , which should be avoided . the process of this invention can be run with a direct current of constant polarity , or the direction of current may be periodically reversed for short time intervals . in practice the current reversal will not normally be required . referring now to the drawing , the process of the present invention can be operated according to the flow sheet therein . a dialkylamine , carbon disulfide and recycled sodium hydroxide are combined to form sodium dialkyldithiocarbamate in the &# 34 ; salt reactor &# 34 ; ( 1 ). to the product from this reactor is added filtrate and wash water ( 2 ) from the final product isolation steps so that unchanged dithiocarbamate can be recovered . these streams are heated in an evaporator ( 3 ) and enough water is evaporated to give a feed stream ( 4 ) to the electrolysis cell anode compartment of the desired dithiocarbamate concentration . since impurities built up in the recycle streams will be at the highest concentration in this stream , a purge ( 24 ) is provided here so that impurity levels will equilibrate . the dithiocarbamate solution is electrolyzed in the anode compartment ( 5 ) of the electrolytic cell which is separated from the cathode compartment ( 6 ) by a cationic membrane ( 7 ). the effluent from the anode compartment ( 8 ) contains precipitated tetraalkylthiuram product . solids in this effluent stream are concentrated in a settling tank ( 9 ) to give dialkyldithiocarbamate solution for recycle ( 10 ) and a more concentrated slurry of product tetraalkylthiuram disulfide ( 11 ). the slurry is filtered and washed with water in filter ( 12 ) to give a wet filter cake product ( 13 ). the filtrate and wash water ( 2 ) are recycled as described above . the wash water ( 14 ) is provided from water storage tank ( 15 ). this tank is supplied by the water evaporated from the evaporator ( 16 ) and needed make - up water ( 17 ). this water supply also furnishes the make - up water for the catholyte ( 18 ) which enters the cathode compartment ( 6 ) along with recycled caustic solution ( 19 ). effluent from the cathode compartment ( 20 ) is degassed in liquid - gas separator ( 21 ) to give by - product hydrogen ( 22 ) and caustic for recycle as catholyte ( 19 ) and for use in the salt reactor ( 23 ). the caustic solution recycled to the cathode compartment contains at most 17 % by weight of sodium hydroxide . this scheme makes a very neat process in which the only outflows from the process are the wet cake product ( 13 ), by - product hydrogen ( 22 ) and a small liquid purge stream ( 24 ). ( 2 ) anode scraping devices are not needed so that standard electrochemical processing equipment can be used . ( 3 ) the sodium hydroxide generated at the cathode is of a high quality and can be recycled to the reactor where the sodium dithiocarbamate salt is formed . this invention is now illustrated by the following examples of certain representative embodiments thereof , where all parts , proportions , and percentages are by weight unless otherwise indicated . a glass electrolysis cell with two 300 ml . compartments separated by a nafion ® type 427 cationic membrane was fitted with two 10 cm 2 electrodes made of 5 mil platinum foil . to the anode compartment was added 300 ml of aqueous solution containing 137 grams of sodium dimethyldithiocarbamate ( 40 % dithiocarbamate ). the catholyte was 300 ml of 0 . 49 n sodium hydroxide . a current of 3 amp was passed through the cell for one hour while the anolyte and catholyte were magnetically stirred . at the end of this time the anolyte was filtered , and pure , white tetramethyl thiuram disulfide with a melting point of 148 . 8 ° c . was recovered . conversion of the sodium dimethyldithiocarbamate was about 10 %. current efficiency was 88 . 5 %. product did not adhere to the anode during this operation . the temperature of the anolyte was measured as 64 ° c . toward the end of the operation . by material balance , 95 . 5 % of the electrolyzed dithiocarbamate was accounted for as the tetramethylthiuram product recovered . this comparative experiment was carried out under the same conditions as example 1 except that a single 300 ml beaker housed both electrodes . no membrane was used in the cell . the beaker was charged with 300 ml of sodium dimethyldithiocarbamate solution . a 3 amp current was passed through the cell for one hour while the solution was magnetically stirred . at the end of this time the solution was filtered to give 2 . 4 grams of product when dry . this is equivalent to 2 . 1 % conversion of the dithiocarbamate present and a current efficiency of about 18 %. conditions of example 1 were reproduced except that a 2 . 5 amp current was passed through the cell for four hours . a pure white product ( 35 . 1 g ) was obtained which had a melting point of 145 ° c . current efficiency was 78 . 3 %. conversion of sodium dimethyldithiocarbamate was about 25 %. thus good product was produced in exmaples 1 and 3 at high current efficiencies at 0 . 25 and 0 . 30 amp / cm 2 current densities . conditions of example 3 were repeated except that the temperature was not allowed to rise to the usual 60 °- 90 ° c . with an ice bath around the anolyte , the temperature was maintained at 20 °- 28 ° c . after a 2 . 5 amp current was passed for 4 hours , 14 . 55 g of a yellow product was recovered by filtration and drying . current efficiency was only 32 . 5 %. this shows the undesirability of operating the electrochemical cell at a temperature well below the stated minimum temperature . the same apparatus and electrolyte solutions as used in examples 1 , 3 and 4 were used here . a lower current of 1 amp was passed for 4 hours . this resulted in 6 . 21 g . of impure product with a melting point of 132 ° c . current efficiency was only 34 . 7 %. it appears desirable to operate at current densities of 0 . 2 amp / cm 2 or greater for satisfactory cell operation rather than at the lower current density ( 0 . 1 amp / cm 2 ) of this example . the same conditions as shown in example 1 were used here . a 3 amp current was passed for 2 hours giving 23 . 5 g . of a white product . anolyte temperature toward the end of cell operation was about 76 ° c . current efficiency was 87 . 4 %. the same apparatus and conditions used in example 6 were used here except that only 27 . 4 g . of sodium dimethyl dithiocarbamate were in the anolyte . thus the solution was only 8 % dithiocarbamate by weight rather than the 40 % normally used . after a 3 amp current was passed through the cell for 2 hrs , 5 . 9 g . of a yellow product were recovered . anolyte temperature had reached 90 ° c . the current efficiency was only 21 . 9 %.