electrodialysis ( ed ) is widely practiced for desalting of aqueous solutions : brackish water , whey milk ( u . s . pat . nos . 3 , 433 , 726 ; 3 , 447 , 930 ; 3 , 595 , 766 ; 3 , 757 , 005 ; 3 , 754 , 650 etc .). these patents are concerned only with reducing the salt content of a liquid rather than using the ed process in a complex scheme of fractionating and subsequently rebalancing the salt and water content of a mixture of proteins intended for example , for therapeutic use as in cases of plasmapheresis . desalting by ion exchange column technology has been used in the past to cause precipitation and thus fractionation of plasma proteins ( u . s . pat . nos . 3 , 234 , 199 ; 3 , 073 , 744 ). this process however has limited flexibility and the columns are difficult to handle , clean and sterilize when employed under conditions necessary for protein fractionation . it has now been discovered that electrodialysis can be used not only in the fractionation of proteins as a result of desalting , but also can be employed in a salting - out process and also in a process to restore the electrolyte ( salt ) and water balance of the resulting processed protein mixtures . the resulting protein is thus ready to be returned to the donor or to a patient with substantially its original salts . the combination of the techniques outlined herein include as essential steps the electrodialysis of the protein mixture , ( optionally combined with temperature and ph alteration ) and separation of certain precipitated proteins , thereafter the optional substantial restoration of the salt and water balance of the original mixture . this novel method increases the efficacy of each step in an unexpected manner and makes the process extremely useful especially for in situ real - time therapeutic use for plasmapheresis patients where removal of globulins or their complexes is required along with the restoration of essentially the original plasma . by this method , not only is the expense of albumin and salt replacement avoided but also the risk of transmitting hepatitis inherent in the giving of fresh or frozen pool plasma . in a first embodiment of fractionation by desalting , process and apparatus will be hereinafter described by referring to fig1 and 2 where like parts are referenced with like numerals . in the figures the fluid under treatment is described with respect to blood plasma but it can be understood to be any other protein mixture . as shown in fig1 citrated or heparinized blood ( 1 ) is ultrafiltered and / or centrifuged ( 2 ) to separate out the cell components ( 3 ), or any other suspension [ referred to as formed elements ( fe )] and the remaining plasma ( 15 ) is sent to an electrodialysis ( ed ) stack ( 4 ) such as that commercially available from ionics , inc . watertown , ma . electrodialysis equipment and their methods of operation are more fully descirbed in u . s . pat . nos . 2 , 848 , 403 ; 2 , 863 , 813 ; 3 , 003 , 940 ; 3 , 341 , 441 ; 4 , 115 , 225 and others . such a stack normally comprises one or more pairs of concentrating and diluting chambers separated by alternating anion and cation exchange membranes . ion selective membranes can also be replaced under some circumstances by essentially electrically neutral membranes . thus the anion membrane can be replaced by a neutral membrane if reduced current efficiency for ionic transfer can be tolerated . the chambers are located between anode (+) and a cathode (-). an electrolyte solution is preferably passed through the cathode and anode chambers to conduct current across the concentrating and the diluting chambers . the electric current is passed until at least incipient turbidity is produced , or until such turbidity will be produced when the temperature is reduced and / or the ph is adjusted to substantially the pi of the least soluble protein . usually a concentrating chamber isolates the electrode solutions from the product or diluting chambers . the membranes are generally but not necessarily selected so as to minimize transfer of low molecular weight compounds such as blood sugars . the flow rates through the stack and the applied electric current are regulated so that excessive changes in ph are avoided . plasma is passed into and through the diluting chambers and by impressing a direct current across the electrodes , the salt or ionic content of the plasma is reduced due to the passage of salt into the adjacent concentrating chambers ( note vertical arrows in stack ) which chambers may be primed if desired initially with a small amount of plasma or albumin . the resulting substantially desalted plasma ( 5 ) is collected from the diluting chambers ( not shown ) and passed into means for separating and removing one or more proteins forming turbidity ( globulins or their complexes in this case ). the separating means may , for example , consist of a heat exchanger ( 6 ) to lower temperatures , ph adjustment and centrifuging and / or ultrafiltration apparatus ( 7 ). after removal of the turbidity or precipitated globulins ( 17 ) or other proteins , the salt depleted mixture ( 8 ) is passed into and through the concentrating chambers ( not shown ) of the ed stack ( 4 ) thereby allowing it to receive the salts from the adjacent diluting chambers ( note vertical arrows ) and hence restoring substantially the original salt content of the mixture . this salt restored mixture ( 9 ) is next optionally passed through a heat exchanger ( 10 ) to adjust the mixture to approximately body temperature where necessary , and then supplied with the formed elements ( e . g . red and white cells and platelets ) ( 3 ) previously separated from the plasma . this restored protein mixture ( 12 ) can then be given back to the patient ( 14 ) substantially without outside addition of albumin or electrolyte . thus this process is essentially closed , self sufficient , and capable of in - situ real - time operation for therapeutic plasma exchange . if the temperature of the plasma during electrodialysis is maintained in the range of about 0 ° to 40 ° c ., if the velocity of the protein mixture in the diluting chambers is in the range of 3 to 40 cm / sec . and the ratio of current density ( cd ) in ma / cm 2 to protein solution conductivity ( k ) in milli siemens / cm ,( cd / k ) is kept in the range of 0 . 1 - 10 , ph changes in the protein will not be substantial and the precipitate so formed ( even on relatively complete desalting ) will be such as to substantially avoid plugging the chambers of the ed stack . ( it should be noted that one mille siemen equals one milli mho . another embodiment of the apparatus and process of this invention is shown in fig2 . the fluid is again plasma ( 1 ) but can be any other aqueous , fluid protein mixture . ( citrate or heparin may or may not be added to minimize plasma coagulation during processing .) the plasma whether or not heparinized or citrated is ultrafiltered or centrifuged ( 2 ) to remove turbidity and then sent to ed stack ( 4 ) similar to that described in example 1 . plasma is introduced into the diluting chambers ( not shown ) and on passing a direct current across the stack , salts from the plasma are transferred ( note vertical arrows ) to the concentrating chambers . the salt depleted mixture ( 5 ) from the diluting chambers is passed through heat exchanger ( 6 ) to chill the plasma and the precipitate formed ( 17 ) is separated by an ultrafilter or a centrifuge ( 7 ) or similar device . the desalted supernatant ( 8 ) is then fed to the salt concentrating chambers ( not shown ) of an electrodialysis stack ( 18 ). for this second ed operation another ed stack ( 18 ) is shown , in practice it can be the original ed stack ( 4 ) where the former concentrating stream ( 19 ) of the ed stack ( 4 ) forms the diluting stream . the polarity for ed stack ( 18 ) may be the reverse of ed stack ( 4 ). this second stage ed ( 18 ) causes the salts from the former concentrating stream ( 19 ) to return to the desalted plasma whereby the salt balance is restored . this renormalized plasma ( 9 ) is then passed through heat exchanger ( 10 ) and the blood cells or fe ( 3 ) are then added . the thus processed blood can be given back to the donor or other patient ( 14 ). this example illustrates the restoration of the electrolyte and water balance of a desalted plasma using a fresh plasma in the dilute stream . apparatus used was a laboratory electrodialysis stack using only one cell pair ( i . e . one diluting and one concentrating chamber defined by ion - selective membranes ) located between terminal electrode chambers . a 0 . 2 n na 2 so 4 solution was used for the electrode streams to conduct the direct current . a volume of 360 ml of citrated otherwise fresh plasma was used in the diluting stream and 340 ml of desalted plasma was used in the concentrating stream . the linear velocity of the diluting stream was about 25 cm / sec ., the temperature was maintained at 15 ° to 20 ° c . and the flow rates at 90 ml . min per cell pair . the effective cell area was about 220 cm 2 . the progress of the run is summarized in the following table : ______________________________________ diluting stream conc . stream ( citrated fresh ( desalted plasma ) plasma ) con - conduc - duc - tivity tivity time values valuescd / k ( min .) amps ( k ) ph vol . ( k ) ph vol . ______________________________________4 . 7 0 17 16 . 500 8 . 2 360 0 . 030 5 . 2 3404 . 7 6 8 . 8 8 . 600 7 . 4 352 8 . 500 7 . 2 3474 . 7 12 4 . 4 4 . 300 6 . 9 347 12 . 400 7 . 7 3505 . 0 25 0 . 9 0 . 825 6 . 1 344 15 . 600 8 . 0 35327 . 5 35 0 . 2 0 . 033 5 . 2 342 16 . 400 8 . 3 355______________________________________ thus the desalted plasma in the concentrating stream has been brought back to a conductivity value comparable to the original unsalted citrated plasma ; and the water balance has been restored . although the ed stack employed in example i contained ion - selective membranes ( anion and cation types ), the combination of ion - selective membranes with neutral ( non - selective ) membranes may also be used . in this example the stack of example i had its anion selective membrane replaced by a neutral membrane comprised of regenerated cellulose . other type neutral membranes well known in the art , such as reverse osmosis or dialysis type membranes could also be used if so desired . neutral membranes have the disadvantage of not being as efficient as as ion - selective membranes . however , in processes where the energy input is not a significant consideration , such membranes can then be utilized to advantage . in this example the stack containing the regenerated cellulose membrane was operated using substantially the same solutions and conditions as noted in example i . the following table summarizes the course of this run : ______________________________________ conc . stream diluting stream______________________________________ ( desalted plasma ) ( fresh plasma ) con - conduc - duc - time tivity tivitycd / k ( min .) amps ( k ) ph vol . ( k ) ph vol . ______________________________________3 . 3 0 12 . 0 16 . 500 8 . 2 360 0 . 050 5 . 3 3403 . 3 14 6 . 2 8 . 700 7 . 4 350 8 . 480 7 . 4 3503 . 3 27 3 . 1 4 . 300 6 . 9 342 12 . 390 7 . 7 3553 . 3 57 0 . 6 0 . 830 6 . 1 337 15 . 450 8 . 0 36023 . 3 80 0 . 2 0 . 039 5 . 2 334 16 . 420 8 . 2 363______________________________________ here again , the desalted plasma has been restored to a conductivity comparable to the original fresh plasma and has also had the water balance restored . it will be noted that the increased time of operation ( 80 minutes ) was due to the current efficiency being considerably less for the combination of neutral and cation exchange membranes . this example is similar to the example i above except that the desalted plasma is used in the original diluting stream of example i and a water solution containing the removed salts from a prior desalting run is used in the original concentrating stream . the polarity of the current is reversed ( thus converting the original concentrating chambers to diluting chambers and the original diluting chambers to concentrating chambers ) and the salts from the salt water stream are transferred to the desalted plasma ( now the concentrate stream ) to bring the salts of the plasma back to its original concentration . this example illustrates the removal of immune globulins ( ig ) as a function of the degree of desalting . the apparatus of example i was used with 200 ml of heparinized human plasma employed in the diluting chamber . the temperature was in the range of 10 °- 26 ° c . and the cd / k value used was approximately 4 ( ma / cm 2 / ms / cm ). a fluid velocity of 25 cm / sec . was employed . the following table summarizes the results and shows that about 50 % of the total ig &# 39 ; s are removed while albumin removal is substantially unaltered after 99 . 7 % desalting . ______________________________________ proteins remaining in supernatanttime conduc - % ( mg / 100 ml )( min .) ph tivity desalting igg iga igm albumin______________________________________0 7 . 55 15 . 280 0 820 115 72 4 , 4100 7 . 55 13 . 720 0 750 85 50 3 , 9005 7 . 35 7 . 020 48 . 80 780 80 46 3 , 9008 7 . 10 3 . 710 72 . 96 700 75 36 3 , 90010 6 . 55 1 . 310 90 . 60 630 75 24 4 , 10013 5 . 40 0 . 447 96 . 70 570 55 12 4 , 00015 5 . 20 0 . 190 98 . 60 450 50 10 4 , 00017 4 . 90 0 . 047 * 99 . 70 410 40 16 3 , 90019 5 . 00 0 . 028 99 . 80 410 45 12 3 , 80020 5 . 10 0 . 022 99 . 84 410 45 10 3 , 800______________________________________ * summary of % ig &# 39 ; s removed after 99 . 7 % desalting % removed ( corrected % removed for water transfer ) ______________________________________igg = 45 . 3 46 . 7iga = 52 . 9 55 . 9igm = 68 . 0 71 . 4total ig &# 39 ; s = 47 . 3 49 . 7______________________________________ this example illustrates a further embodiment of the invention , where alteration of ph to substantially the isoelectric point of a protein which it is desired to remove can assist its precipitation . continuation of the desalting of the plasma resulting from example iv will bring the ph down to the isoelectric point ( pi ) of albumin ( about 4 . 9 ) thus causing its precipitation . the albumin precipitate is separated by filtration and then resuspended by the addition of salt . this addition is accomplished using ed by making the albumin rich material as the salt concentrating stream thus resulting in a 3 - 5 % isotonic albumin solution . this albumin is essentially free of immunoglobulins and their complexes and can be used as a plasma expander . thus this is a preferred method for those cases where more than 40 - 50 % removal of immune globulins is desirable for &# 34 ; immunepheresis &# 34 ; ( removal of immunoglobulins ) for autoimmune diseases . in another embodiment of the invention , fractionation is achieved by &# 34 ; salting - out &# 34 ; i . e . the use of salts such as ( nh 4 ) 2 so 4 , na 2 so 4 etc . brought into the protein mixture by electrodialysis . the various proteins will precipitate out at different salt concentrations and thereby lend themselves to fractionation . a distinct advantage of accomplishing this by ed instead of by direct addition of salts is that ed allows more controlled addition of salts , thus avoiding local concentration gradients . electrodialysis &# 34 ; salting - out &# 34 ; is also much faster when compared to dialysis alone where only diffusion ( and not an electric potential ) is the driving mechanism . comparable fractionation is achieved by ed at a much lower salt content compared to either addition or dialysis addition of salt . the process and apparatus employed for salting - out will be further described hereinafter for the fractionation of blood plasma protein but is not to be understood as limited to plasma only . two of the &# 34 ; salting - out &# 34 ; embodiments are shown in fig3 and 4 . as shown in fig3 fresh plasma ( 15 ) is pumped as the concentrating stream ( salt receiving stream ) through two electrodialysis stacks ( 4 ) and ( 11 ). the resulting salted - out plasma ( 22 ) is passed into separation means ( 7 ) such as a centrifuge where removal of any precipitated protein ( 17 ) is accomplished . the resulting supernatant ( 8 ) which becomes the diluting stream to the ed stack ( 11 ) is essentially an albumin filtrate containing the salting out agent ( such as na 2 so 4 ) from which a precipitated protein fraction ( 17 ) has been removed ( e . g . immunoglobulins and fibrinogen ). this stream is made to give up its salt ( note the direction of vertical arrows ) when a current is impressed across the ed stack , that is , transfer the salting - out agent to a fresh plasma stream ( 15 ) thus causing the precipitation of certain proteins ( globulins ) from said fresh plasma stream . in turn this dilute stream ( 8 ) becomes depleted of salt and becomes essentially an albumin solution . the final or polishing ed stack ( 4 ) is shown separately but it can be part of a single ed stack . this final polishing step may not be required where the product ( 9 ) is allowed to have salts which are not objectionable for infusion . a make up electrolyte ( 20 ) may be needed if the polishing ed step is required . thus such a process is compatible with in situ operation for therapeutic plasma exchange and can be carried out not only in batches but also continuously . another variation of the salting - out embodiment of this invention is shown in fig4 . here the salting - out agent ( salt solution ) is added directly to the plasma ( 15 ) causing immunoglobulins to precipitate whereby they are separated ( 7 ) and removed ( 17 ) as by filtration . the resulting plasma ( 16 ) employed as the dilute stream is desalted by ed stack ( 4 ); with the concentrating stream ( 18 ) becoming essentially a solution of the salting - out agent . this concentrated solution ( 19 ) can be added directly to fresh plasma ( 15 ) in a closed loop fashion . electrolytes ( 20 ) and formed elements ( 3 ) may be added to the desalted albumin solution ( 9 ) before administering the solution ( 12 ) back to the donor or patient ( 14 ). although na 2 so 4 is preferred as the salting - out agent it must be understood that this invention is not limited to it . other salts and their mixtures may be used such as k 2 so 4 , ( nh 4 ) 2 so 4 , sodium citrate , phosphates , nacl , kcl , acetates , etc . and their mixtures . the amount of salt added will of - course depend upon the fractionation desired . the following example illustrates the separation of igg from albumin . 300 ml of plasma was warmed to 28 °- 37 ° c . and a saturated solution of na 2 so 4 ( approximately 6 n ) at 28 °- 37 ° c . was added at a rate of 10 - 15 ml / min . while constantly and rapidly stirring the plasma mixture . the amount of albumin and globulins ( igg ) remaining in the supernatant was determined during the salt addition as a function of salt ( electrolyte ) concentration in the supernatant . fig5 compares the results using various methods of adding na 2 so 4 electrolyte and shows the approximate protein fractionation ( albumin and igg &# 39 ; s ) occurring at different electrolyte strengths . also specifically shown is the fractionation curve resulting when a salt mixture ( 6 n nacl and 6 n na 2 so 4 ) was employed . a comparison of salting - out by electrodialysis , dialysis and direct salt addition is also illustrated . the results show that to obtain about 80 % removal of globulins ( igg &# 39 ; s ) from fresh plasma requires a 1 . 8 n . salt ( na 2 so 4 ) concentration in the plasma ( supernatant ) in the case where direct salt addition is employed . under these conditions however , there was also a simultaneous removal ( a loss ) of about 15 % albumin . where the direct addition employed a salt mixture ( na 2 so 4 + nacl ) an 80 % removal of globulins occurred at about a 2 . 05 salt normality accompanied by only a 5 % removal of albumin . where the addition of salt ( na 2 so 4 ) is accomplished by use of dialysis an 80 % globulin removal was noted at about a 2 . 3 salt normality but at a loss of about 10 % albumin . in comparing the use of salt addition by electrodialysis ( ed ) it is noted that there is a 95 % removal of globulins at a much lower salt normality ( 1 . 2 n ) with less than 15 % loss of albumin . in summary it appears that more complete removal of globulins accompanied with smaller losses of albumin can be accomplished at the lower salt normalities when the salt addition is performed by electrodialysis . an alternate procedure where so desired is to employ a combination of direct addition or dialysis of the salting out agent thereafter followed by ed treatment to remove the added salts therefrom . this example illustrates the separation of antihemophilic factor ( ahf ) and fibrinogen from the plasma . since the activity of ahf is time and temperature sensitive , the separation is carried out at a low temperature ( 4 ° c .). one procedure applied in the separation is lowering the ionic strength of plasma preferably by ed desalting to cause the precipitation ( separation ) of fibrinogen and ahf , later resolubilizing the precipitate in for example , 0 . 15 n nacl and thereafter subjecting the resulting resolubilized liquid once again to ed to lower the ionic strength thus causing the precipitation ( and separation ) of ahf from fibrinogen . alternatively after resolubilizing , the latter separation can be caused by specific adsorption of ahf on anion exchange column or by gel permeation techniques . a second procedure consists of the direct salting out of ahf at an appropriate salt strength . these procedures are also applicable for on line as well as off line use as in the case of immunepheresis . another embodiment of this invention is the application of ed to the fractionation of plasma proteins using small amounts of low toxicity heavy metal ions such as zinc diglycinate as the precipitating agent . the plasma is first partially electrodialyzed to remove clotting factors which become precipitated during the desalting . these precipitated factors are removed and the resulting supernatant is passed through the salt concentration compartments of an ed stack containing zinc diglycinate in the diluting compartments . on application of a electrical potential a controlled amount of zinc diglycinate is transferred into the concentrating compartments to give an ionic strength of about 0 . 10 normal in the supernatant . the operation is carried out at about 0 °- 4 ° c . and at a ph of about 7 . 0 - 7 . 2 . this results in the formation of a precipitate consisting essentially of globulins with a supernatant rich in albumin . the supernatant can be clarified of the added zinc by desalting by ed after bringing the ph down to about 5 . 1 - 5 . 8 by suitable addition of a buffer . aluminum chloride may also be substituted for zinc diglycinate for fractionally precipitating all proteins except γ - globulins . the direct addition of an equal volume of 0 . 1 m alcl 3 at 0 ° c . to plasma with rapid stirring will precipitate all other proteins which may then be redissolved in 0 . 15 n . nacl . this example illustrates the use of alternating current rather than the use of direct current which is normally employed in electrodialysis operations . the stack employed a combination of neutral ( n ) and cation - selective ( c ) membranes in an arrangement illustrated in fig6 . an alternating current ed stack is fully described in u . s . pat . no . 2 , 955 , 999 ( c . e . tirrell ). a valve metal such as niobium ( 4 ) plated with a noble metal such as platinum ( 5 ) is used as an anode ( 1 ) and the valve metal ( 6 ) without the coating of a noble metal is used as a cathode ( 3 ). the valve metals have the property of conducting current only when they are made cathodic , hence effecting a sort of &# 34 ; rectification &# 34 ; of the alternating current ( ac ). such a stack uses two cell pairs ( instead of one as used in example ii ) separated by a middle bipolar electrode ( 2 ) platinized ( 5 ) one one side to serve as an anode . during the positive (+) current half cycle the platinized side ( 5 ) of electrode ( 1 ) serves as the anode and the unplatinized side ( 4 ) of electrode ( 2 ) as cathode and hence the membrane stack bound by electrodes ( 1 ) and ( 2 ) is in service whereas the membrane stack between electrodes ( 2 ) and ( 3 ) is inactive since electrode ( 3 ) being unplatinized cannot function as an anode . during the negative (-) current half cycle the stack between electrodes ( 2 ) and ( 3 ) is functional since the platinized side ( 5 ) of electrode ( 2 ) is anode . such a stack operates in a similar fashion as that of example ii . the apparatus will have the advantage of being operated from alternating current obviating the necessity of a rectifier . the neutral membrane can also be replaced by an anion membrane to make the operation more energy efficient . this example illustrates the removal of factor viii from human plasma by employing electrodialysis for the desalting . the membrane separation apparatus used is a dial - a - cell ™ stack commercially available from ionics , inc . of watertown , mass . and is fully described in u . s . pat . no . 4 , 202 , 772 . the stack comprised two cell pairs having an effective membrane area of 13 . 6 cm 2 . the ion - exchange membranes used were the cation selective ( cr 61 czl ) and anion selective types ( ar 103 qzl ) both also obtainable from ionics , inc . 30 ml of fresh plasma containing acd ( anticoagulant solution consisting of a mixture of sodium citrate , citric acid and dextrose ) was used in this run . the starting plasma had a factor viii activity of 78 % of the normal . the following table summarizes the results of the desalting run . as the plasma is desalted , factor viii is precipitated out and hence the supernatant is depleted in factor viii . at about the 90 % desalting level the supernatant retains about 5 - 10 % of factor viii , hence the removed precipitate would contain about 90 - 95 % of the factor viii originally contained in the starting plasma sample . ______________________________________time conductivity factor viii activity in ( min .) ( k ) % desalting supernatant (% or normal ) ______________________________________ 0 13 . 6 0 7812 11 . 6 14 . 7 7018 8 . 4 38 . 2 6324 6 . 4 52 . 9 4230 3 . 6 47 . 6 3033 2 . 8 79 . 4 936 2 . 2 83 . 8 1239 1 . 8 86 . 8 542 1 . 0 92 . 6 11______________________________________ the treatment of liquid whey to increase the desirable protein content and decrease the ash ( salt ) and lactose components has been the object of a variety of processes . l . h . francis in u . s . pat . no . 3 , 615 , 664 discloses a technique in which lactose is removed from whey by concentration of the raw whey to crystallize lactose and then subjecting the supernatant to electrodialysis to effect demineralization . the same inventor in u . s . pat . no . 3 , 447 , 930 describes another process where demineralizing is done first followed by delactosing . these and other prior art methods are directed to the purpose of obtaining a refined high protein whey end product . some of the major concerns in carrying out these processes are denaturation of whey protein ( lactalbumin ) during the application of heat to effect concentration and crystallization . the process of the present invention is to overcome these problems by salting - out the whey proteins , followed by the separation and removal of the precipitated proteins by centrifugation or filtration and thereafter removal of the salt from the resulting supernatant . the supernatant will be comprised mainly of lactose and hence can be subjected to high temperatures without fear of protein denaturation . it should be noted that this process not only separates the proteins but also effects desalting by methods previously described in examples directed to plasma protein treatment . the ed apparatus used is similar to the one described in example i . the diluting stream is comprised of 500 ml . of supernatant obtained from a prior whey run where substantially all whey proteins were removed i . e . salted - out by electrodialysis at about a 3 . 5 sodium sulfate normality at an operating temperature of about 38 ° c . 300 ml of concentrated whey with a solid content of 22 . 5 % ( solids = 12 % proteins , 80 % lactose hydrate and about 8 . 0 % ash ) is used as the concentrating stream . a direct current density of about 130 asf is used ( starting cd / k = 2 . 0 ) and near the end of the run where the diluting stream becomes depleted of much of its salts , the current is adjusted to conform to a cd / k of about 4 . 8 . the run is continued until a normality of about 3 . 5 na 2 so 4 is obtained in the concentrating stream where the conductivity is about 95 milli siemens / cm . the diluting stream volume which is reduced to about 300 ml is 90 % salt free and may be further treated to recover lactose . the concentrating stream which increases in volume to about 500 ml develops a fine precipitate ( turbidity ) of protein which is removed by centrifugation . the resulting highly salted supernatant is then used as the diluting stream to transfer its salting - out agent to a next fresh batch of concentrated whey . this method of transfering the salting - out agent is accomplished in a manner similar to the cases of human plasma protein separation as described previously . while the invention has been herein shown and described in what is presently conceived to be the most practical and preferred embodiments thereof , it will be apparent to those of ordinary skill in the art that many modifications may be made thereof within the scope of the invention , which scope is to be accorded the broadest interpretation of the appended claims so as to encompass all equivalent assemblies and methods .
this invention relates to the separation of complex protein mixtures by lowering or by raising their electrolytic concentration by electrodialysis followed by chilling , ph adjustment , filtration , and / or centrifugation and optionally thereafter restoration of the lost electrolyte or removal of the gained electrolyte and water . this technique is especially adaptable for therapeutic plasma exchange performed in situ for immunepheresis i . e . removal of globulin or immunecomplexes implicated in autoimmune diseases . the techniques are also applicable for antihemophilic factor separation and purification , and separation of proteins from whey .