Background Art The modern biotechnology industrv is faced with a number of problems especiallv concerning the processing of complex biological solutions which ordinarilv include proteins. nucleic acid molecules and complex sugars and which are contaminated with unwanted biological materials. Contaminants include microorganisms such as bacteria and viruses or biomolecules derived from microorganisms or the processing procedure. The demand is. therefore, for a high purity. scalable separation, which can be confidentlv used both in product development and production, which in one step will both purify macromolecules and separate these biologicalcontaminants.

Viruses are some of the smallest non-cellular organisms known. These simple parasites are composed of nucleic acid and a protein coat. Viruses are typically very small and range in size from 1.5xl0-8 m to 5. 0x10-5 m. Viruses depend on the host cells that they infect to reproduce by inserting their genetic material into the host. often literally taking over the host's function.

An infected cell produces more viral protein and genetic material, often instead of its usual products. Some viruses may remain dormant inside host cells. However. when a dormant virus is stimulated. it can enter the lytic phase where new viruses are formed. self-assemble occurs and burst out of the host cell results in killing the cell and releasing new viruses to infect other cells. Viruses cause a number of diseases in humans including smallpox. the common cold. chicken pox. influenza. singles. herpes, polio. rabies. Ebola. hanta lever, and AIDS. Some types of cancer have been linked to viruses.

Pvrogens are agents which induce fever. Bacteria are a common source for the production of endotoxins which are pyrogenic agents. Furthermore. another detrimental effect of endotoxins is their known adjuvant effect which could potentially intensifv immune responses against therapeutic drugs. The endotoxin limit set by the Food and Drug Administration (FDA) guidelines for most pharmaceutical products is for a single dose 0.5ng endotoxin per

kilogram bodv weight or 25ng endotoxin/dose for a 50kg adult. Due to their size and charge heterogeneitv, separation of endotoxins from proteins in solution can often be difficult. Endotoxin inactivation by chemical methods are unsuitable because they are stable under extremes of temperature and pH which would destroy the proteins. Furthermore. due to their amphipathic nature. endotoxins tend to adhere to proteins in a fashion similar to detergents. In such cases, endotoxin activity often clusters with the protein when chromatographic procedures such as ion exchange chromatography or gel filtration are employed.

Presentlv the purification of biomolecules is sometimes a long and cumbersome process especially when purifying blood proteins. The process is made all the more complex by the additional step of ensuring the product is"bug"free. The costs associated with this task is large and further escalates the purification costs in total. The Gradiflow technology rapidly purifies target proteins with high yield. For example, a proteins like fibrinogen (a clotting protein) can be separated in three hours using the Gradiflow while the present industrial separation is 3 days. Certain monoclonal antibodies can be purified in 35 minutes compared to present industrial methods which take 35 hours.

The membrane configuration in the Gradiflow enables the system to be configured so that the purification procedure can also include the separation of bacteria viruses and vectors. It has now been found by the present inventors that appropriate membranes can be used and the cartridge housing the membrane configured to include separate chambers for the isolated bacteria and viruses.

The Gradiflow Technology Gradiflow is a unique preparative electrophoresis technology for macromolecule separation which utilises tangential flow across a polvacrvlamide membrane when a charge is applied across the membrane (AU 601040). The general design of the Gradiflow system facilitates the purification of proteins and other macromolecules under near native conditions. This results in higher yields and excellent recovery.

In essence the Gradiflow technology is bundled into a cartridge comprising of three membranes housed in a system of specially engineered grids and gaskets which allow separation of macromolecules by charge and/or molecular weight. The system can also concentrate and desalt/dialyse at the

same time. The multimodal nature of the system allows this technology to be used in a number of other areas especially in the production of biological components for medical use. The structure of the membranes may be configured so that bacteria and viruses can be separated at the point of separation-a task which is not currentlv available in the biotechnology industrv and adds to the cost of production through time delavs and also because of the complexitv of the task.

Disclosure of Invention In a first aspect. the present invention consists in a method of removing a biological contaminant from a mixture containing a biomolecule and the biological contaminant, the method comprising: (a) placing the biomolecule and contaminant mixture in a first solvent stream. the first solvent stream being separated from a second solvent stream by an electrophoretic membrane: (b) selecting a buffer for the first solvent stream having a required pH; (c) applying an electric potential between the two solvent streams causing movement of the biomolecule through the membrane into the second solvent stream while the biological contaminant is substantially retained in the first sample stream. or if entering the membrane. being substantially prevented from entering the second solvent stream : (d) optionally. periodicallv stopping and reversing the electric potential to cause movement of anv biological contaminants having entered the membrane to move back into the first solvent stream. wherein substantially not causing any biomolecules that have entered the second solvent stream to re-enter first solvent stream: and (e) maintaining step (c), and optional step (d) if used, until the second solvent stream contains the desired puritv of biomolecule.

In a second aspect. the present invention consists in a method of removing a biological contaminant from a mixture containing a biomolecule and the biological contaminant, the method comprising: (a) placing the biomolecule and contaminant mixture in a first solvent stream. the first solvent stream being separated from a second solvent stream bv an electrophoretic membrane: (b) selecting a buffer for the first solvent stream having a required pH: (c) applying an electric potential between the two solvent streams causing movement of the biological contaminant through the membrane into the

second solvent stream while the biomolecule is substantiallv retained in the first sample stream. or if entering the membrane. being substantially prevented from entering the second solvent stream: (d) optionally. periodicallv stopping and reversing the electric potential to cause movement of anv biomolecule having entered the membrane to move back into the first solvent stream. wherein substantially not causing any biological contaminants that have entered the second solvent stream to re- enter first solvent stream: and (e) maintaining step (c). and optional step (d) if used, until the first solvent stream contains the desired puritv of biomolecule.

In the first and second aspects of the present invention. preferably the biomolecule is selected from the group consisting of blood protein. immunoglobulin. and recombinant protein.

The biological contaminant can be a virus, bacterium, prion or an unwanted biomolecule such as lipopolysaccharide. toxin or endotoxin.

Preferably, the biological contaminant is collected or removed from the first stream.

Preferably. the buffer for the first solvent stream has a pH lower than the isoelectric point of biomolecule to be separated.

In a further preferred embodiment of the first aspect of the present invention, the electrophoretic membrane has a molecular mass cut-off close to the apparent molecular mass of biomolecule. It will be appreciated. however. that the membrane may have any required molecular mass cut-off depending on the application. Usuallv. the electrophoretic membrane has a molecular mass cut-off of between about 3 and 1000kDa. A number of different membranes may also be used in a desired or useful configuration.

The electric potential applied during the method is selected to ensure the required movement of the biomolecule. or contaminant if appropriate, through the membrane. An electric potential of up to about 300 volts has been found to be suitable. It will be appreciated. however. that greater or lower voltages may be used.

The benefits of the method according to the first aspect of the present invention are the possibilitv of scale-up. and the removal of biological contaminants present in the starting material ivithout adverselv altering the properties of the purified biomolecule.

In a third aspect. the present invention consists in use of Gradiflow in the purification or separation of biomolecule from a biological contaminant.

In a fourth aspect. the present invention consists in biomolecule substantially free from biological contaminants purified by the method according to the first aspect of the present invention.

In a fifth aspect. the present invention consists in use of biomolecule according to the third aspect of the present invention in medical and veterinary applications.

In a sixth aspect. the present invention consists in a substantially isolated biomolecule substantially free from biological contaminants.

Throughout this specification, unless the context requires otherwise, the word"comprise". or variations such as"comprises"or"comprising", will be understood to imply the inclusion of a stated element, integer or step, or group of elements. integers or steps, but not the exclusion of any other element, integer or step, or group of elements, integers or steps.

In order that the present invention may be more clearly understood a preferred forms will be described with reference to the accompanying drawings.

Brief Description of Drawings Figure 1. Samples from up and downstream were taken at time intervals (x-axis) during the isolation of albumin from plasma. Albumin was measured in the samples by mixing with BCG reagent and reading the absorbance of 630nul11. The concentration of albumin in each sample was calculated from the standard curve. and multiplied by the volume of the up- or downstream to obtain the Total HSA in the up-and downstream (y-axis).

All samples were assayed for prion using a sandwich ELISA. and recording the absorbance values at 450nm (second y-axis).

Figure 2. Samples from the second phase of an IgG separation were taken from both up-and downstreams (U/S and D/S respectively) at 30 minute intervals. The samples were assayed for endotoxin using a LAL Chromogenic assay (Cape Cod Assoc.) Figure 3. HSA was purified from endotoxin spiked plasma. Samples were taken from up-and downstream at 30 minute intervals during a 90 minute purification (x-axis). Analysis of the samples using a LAL Chromogenic assav was performed to establish the endotoxin concentration (y-axis) in the samples.

Figure 4. Four to 25% native gel electrophoresis of samples from an HSA purification from endotoxin spiked plasma. Lane 1 contains molecular weight markers. Lane 2 contains starting plasma sample, Lanes 3-5 contain upstream samples at time 30.60. and 90 minutes. Lanes 6-9 contain downstream samples at time 0.30.60 and 90 minutes. respectively.

Modes for Carrying Out the Invention Virus removal during plasma protein purification using Gradiflow technology Contamination with virus is a major concern when purifying plasma proteins. such as IgG and human serum albumin (HSA). A contaminant virus can potentiallv infect a patient receiving the contaminated plasma products. A virus that infects bacteria is known as a phage, and they are readilv detected bv examining culture plates for cleared zones in a coating or lawn of bacteria.

.-lim: To isolate IgG. HSA, and Fibrinogen from human plasma spiked with virus, using the Gradiflow. with simultaneous removal of the contaminating virus.

IgG purificatiori procedure IgG is the most abundant of the immunoglobulins. representing almost 70% of the total immunoglobulins in human serum. This class of immunoglobulins has a molecular mass of approximately 150kDa and consists of 4 subunits. two of which are light chains and two of which are heavv chains. The concentration of IgG in normal serum is approximately lolllgíml IgGs are conventionallv purified using Protein A affinity columns in combination with DEAE-cellulose or DEAE-Sephadex columns. The main biological contaminants in IgG isolations are ß-lipoprotein and transferrin.

The product of conventional protein purification protocols is concentrated <BR> <BR> using ultrafiltration. Immunoaffinitv can also be used to isolate specific<BR> <BR> IgGs.

. \lethod : Platelet free plasma was diluted one part in three with Tris- borate. pH 9.0 running buffer and placed in the upstream of Gradiflow and spiked with either Llambda or T7 phage to a concentration of-108pfu/ml (plaque forming units/ml). A potential of 250V was placed across a separating membrane with a molecular weight cut off of 200kDa (3kDa restriction membranes). A membrane of this size restricts IgG migration

whilst allowing smaller molecular weight contaminants to pass through the membrane. leaving IgG and other large molecular weight proteins in the upstream. A second purification phase was carried out using a GABA/Acetic acid buffer. pH 4.6 with a 500kDa cut off separating membrane (3kDa restriction membranes). A potential of 250V reversed polarity was placed across the system resulting in IgG migration through the membrane leaving other high molecular weight contaminants upstream.

Examination of samples taken at 30 minutes intervals was made on reduced SDS-PAGE 4-25% gels.

Virustesting One hundred and fifty p1 taken at each time point sample was mixed with 100ul of appropriate Escherichia coli culture (Strain HB101 was used for T7 and strain JIsI101 for Llambda). The mixtures were incubated for 15 minutes at 37"C. before each was added to 2.5ml of freshly prepared molten soft agar. and vortexed. The mixtures were poured over culture plates of Luria Agar. and incubated at 37°C overnight. The plates were inspected for the presence of virus colonies (plaques) in the lawn of E. coli. The number of plaques was recorded or if the virus had infected the entire E. coli population the result was recorded as confluent lysis.

HSA purification procedure Albumin is the most abundant protein component (50mg/m.) in human plasma and functions to maintain blood volume and oncotic pressure.

Albumin regulates the transport of protein. fatty acids. hormones and drugs in the body. Clinical uses include blood volume replacement during surgery, shock. serious burns and other medical emergencies. Albumin is 67kDa and has an isoelectric point of approximately 4.9. The protein consists of a single subunit and is globular in shape. About 440 metric tons of albumin is used annually internationally with worldwide sales of US$1.5 billion. Albumin is currently purified using Cohn fractionation and commercial product contains manv contaminants in addition to multimers of albumin. The high concentration, globular nature and solubilitv of albumin make it an ideal candidate for purification from plasma using Gradiflow technology.

Metliod : Pooled normal plasma was diluted one in three with Tris-Borate (TB) running buffer. pH 9.0 and spiked with ~108pfu/nll of Llambda or T7 phage. The mixture was placed in the upstream of a Gradiflow apparatus.

Albumin was isolated from platelet free plasma in a one-phase process using

the charge of albumin at a pH above its isoelectric point (pI) and its molecular weight. Thus a cartridge with a 75kDa cutoff separation membrane was placed between two 50kDa cutoff restriction membranes.

The albumin was removed from high molecular weight contaminants by its migration through the separation membrane whilst small molecular weight contaminants dissipated through the 50kDa restriction membrane. Samples were taken at regular intervals throughout a 90 minutes run.

The presence of the purified HSA in the downstream was demonstrated bv examination bv SDS-PAGE. Virus was detected as previously described above.

Fibrinogen purificationprocedure: Commerciallv. fibrinogen has a role as fibrin glue. which is used to arrest bleeding and assist in the wound healing process. Fibrinogen is an elongated molecule of 340kDa that consists of three non-identical subunit pairs that are linked bv a disulphide knot in a coiled coil conformation. The isoelectric point of fibrinogen is 5.5 and it is sparingly soluble when compared with other plasma proteins.

Fibrinogen is conventionally purified from plasma by a series of techniques including ethanol precipitation, affinity columns and traditional electrophoresis. This process takes about 48-72 hours and the harsh physical and chemical stresses placed on fibrinogen are believed to denature the molecule. resulting in activity that is removed from that of fibrinogen in plasma.

Cryo-precipitation is the first step in the production of factor VIII and involves the loss of most of the fibrinogen in plasma. Processing of this waste fibrinogen is of considerable interest to major plasma processors and provides an opportunity to demonstrate the rapid purification of fibrinogen from cryo-precipitate using the Gradiflow.

Hethod : Cryo-precipitate 1. produced by thawing frozen plasma at 4°C overnight was removed from plasma by centrifugation at 10000xg at 4°C for 5 minutes. The precipitate was re-dissolved in Tris-Borate buffer (pH 9.0) and placed in the upstream of a Gradiflow apparatus. The upstream was spiked with either Llambda or T7 phage to a concentration of ~ 108pfulnll. A<BR> <BR> <BR> potential of 250V was applied across a 300kDa cutoff cartridge and run for 2 hours. The downstream was replaced with fresh buffer at 30 minute intervals. A second phase was used to concentrate the fibrinogen through a

500kDa cutoff separation membrane at pH 9.0. The downstream was harvested at 60 minutes. The product was dialyse against PBS pH 7.2 and analyse for clotting activity by the addition of calcium and thrombin (final concentrations 10mM and 10NIH unit/ml respectively).

The presence of purified fibrinogen was confirmed by examination on reduced SDS PAGE 4-25% gels. The presence of either T7 or Llambda in the time point samples was tested using the previously described method.

Results of IgG, HSA and fibrinogen purification : The procedures described successfully purified IgG, albumin and fibrinogen as judged bv electrophoresis. Neither T7 nor Llambda phage were detected in the downstream products, but were present in the upstream samples.

Prion removal during plasma protein purification using Gradiflow technology There is an international concern regarding the contamination of plasma proteins by prion protein. Prion is a glycoprotein of 27-33kDa in size which occurs naturally in many human derived materials, including white blood cells, platelets. plasma and plasma proteins preparations, e. g. HSA, IgG. FVIII and fibrinogen. Prion can become folded abnormally and cause neurological disorders such as Creutzfeld-Jacob disease (CJD) and Kuru.

Currently, there is much concern regarding the transmission of these diseases via transfusion and plasma protein fractions administered clinically.

A: To isolate HSA from human plasma using the Gradiflow. with simultaneous removal of prion.

Method: Pooled platelet rich plasma was diluted one in two with Tris- Borate (TB) running buffer. pH 9.0 and was placed in the upstream of a Gradiflow apparatus. Albumin was isolated from platelet free plasma using the charge of albumin at a pH above its pI and its molecular weight. Thus a cartridge with a 75kDa cutoff separation membrane was placed between two 50kDa cutoff restriction membranes. The albumin was removed from high molecular weight contaminants by its migration through the separation membrane whilst small molecular weight contaminants dissipated through the 50kDa restriction membrane. Samples were taken at 20 minute intervals <BR> <BR> <BR> throughout a 240 minute run. The buffer stream and cartridge were replaced after the initial two hours. with identical solutions and cartridge.

The presence of the purified HSA in the downstream was demonstrated by examination by SDS-PAGE. and was measured using a Bromocresol Green Assay (purchase from Trace Scientific. Prion was tested for in both up-and down-stream samples using a sandwich ELISA comprised of prion specific antibodies obtained from Prionics Inc (Switzerland).

Albuminquantitation Fiftv 1 of each time point sample was diluted with 50µl of PBS buffer.

A 20µl aliquot of each diluted sample was placed in a microplate well. A standard curve of the kit calibrator from a maximum concentration of 40mg/ml was prepared using PBS as the diluent. The standard curve dilutions were also placed in the microplate (2µl plasma/well). The bromocresol green reagent was added to all the wells (200111/well) and the absorbance at 630nm was read using a Versamax microplate reader. The standard curve was drawn on a liner scale and the concentration of albumin in the up and downstream samples were read from the curve. The volume in the appropriate stream at the time of sampling was multiplied by the concentration of each sample. Thus providing a value for the total HSA present in each stream.

Prion detection A solution of 5µg/ml monoclonal antibody denoted 6H4 (Prionics Inc.

Switzerland) in a 10mM carbonate buffer was added to the wells of a microplate (1001/well). and incubated overnight at 4"C. The antibody was later decanted and the wells washed three times with 250µl/well of a PBS solution containing 0.1% (v/v) Tween 20. The plate wells were blocked by incubating at room temperature for 30 minutes with 2001/well of PBS/T20 containing 1% albumin. The plate was again washed three times with 2501/well of PBS/T20 before the up-and down-stream time point samples were added (100 vell). The samples were incubated for 1-2 hours at room temperature before being dispense. and the plate washed three times as previously described. A solution of prion-specific polyclonal antibody. denoted R029 (Prionics Inc. Switzerland) was diluted at 1: 1000 (v: v) in PBS/T20. and added to the wells of the plate (100p1/well). The mixture was incubated for 1-2 hours at room temperature. before being decanted. The plate was washed three times and 100µl/well of a horseradish peroxidase conjugated polvclonal anti-rabbit IgG antiserum (purchased from Dakopatts) was added. The conjugate was incubated for 30-60 minutes at room

temperature and then removed. Anv bound HRP conjugate was detected <BR> <BR> using o-tolidine substrate solution (100ul/well). and the reaction stopped by addition of 3NI HCI (501l1/well). The developed colour was measured at 450nu in a Versamax plate reader.

Results Albumin was transferred to the downstream and was detected in the BCG assay (Figure 1). and visualized on a native 8-16% electrophoresis gel.

Decreasing quantities of Prion were detected in the upstream during the time-course. and no Prion was detected in the downstream samples.

Endotoxin removal during plasma protein purification using Gradiflow technology Contamination with bacterial endotoxin is a major concern when purifying plasma proteins. such as IgG and HSA. Endotoxins are a lipopolvsaccharide derived from the lipid membrane of gram negative bacteria. The presence of endotoxin in a human blood fraction therapeutic can lead to death of the receiving patients.

Aim: To isolate IgG and HSA from human plasma spiked with endotoxin, using the Gradiflow, with simultaneous removal of endotoxin.

IgG purification procedure Method. Platelet free plasma was diluted one part in three with Tris- borate. pH 9.0 running buffer and placed in the upstream of a Gradiflow apparatus and spiked with purified E. coli endotoxin to a concentration of 55ngílll1. A potential of 250V was placed across a separating membrane with a molecular weight cut off of 200kDa (3kDa restriction membranes). A membrane of this size restricts IgG migration whilst allowing smaller molecular weight contaminants to pass through the membrane. leaving IgG and other large molecular weight proteins in the upstream. A second purification phase was carried out using a GABA/Acetic acid buffer, pH 4.6 with a 500kDa cut off separating membrane (3kDa restriction membranes). A potential of 250V reversed polaritv was placed across the system resulting in IgG migration through the membrane leaving other high molecular weight contaminants upstream.

Examination of samples taken at 30 minutes intervals was made on reduced SDS-PAGE 4-25% gels. Endotoxin was tested for using a LAL Pvrochrome Chromogenic assav purchased from Cape Cod Associates. All

samples were diluted 1 in 10 and the endotoxin assay was performed according to the manufacturer instructions.

HSA purification procedure . \/lethod: Pooled normal plasma was diluted one in three with Tris-Borate (TB) running buffer, pH 9.0 and spiked with 55ng/ml of purified endotoxin.

The mixture was placed in the upstream of a Gradiflow apparatus. Albumin was isolated from platelet free plasma in a one-phase process using the charge of albumin at a pH above its pI and its molecular weight. Thus a cartridge with a 75kDa cutoff separation membrane was placed between two 50kDa cutoff restriction membranes. The albumin was removed from high molecular weight contaminants bv its migration through the separation membrane whilst small molecular weight contaminants dissipated through the 50kDa restriction membrane. Samples were taken at regular intervals throughout a 90 minutes run.

The presence of the purified HSA in the downstream was demonstrated by examination by SDS-PAGE. Endotoxin was tested for in both up-and down-stream samples using a LAL Chromogenic assay supplied by Cape Cod Associates. All samples were diluted 1 in 10 and the endotoxin assay was performed according to the manufacturer instructions.

Results of IgG and HSA purification Up and downstream samples taken at 30 minute intervals during the second phase of an IgG purification from endotoxin spiked plasma were tested for endotoxin using a LAL Chromogenic assav. The results showed that the endotoxin was almost entirely found in the upstream at all time points (Figure 2). The downstream contained only 0.7% of the initial endotoxin. Reduced SDS-PAGE examination showed that IgG had been successfully isolated in the downstream.

Analvsis of samples taken at 30 minute intervals during the purification of HSA from plasma spiked with endotoxin found the majority of endotoxin remained in the upstream. Only 4% of the total endotoxin was found in the downstream at the end of the run (Figure 3). Native PAGE examination confirme the presence of purified HSA in the downstream samples (Figure 4).

Bacteria removal during plasma protein purification using Gradiflow technology Contamination with bacteria is a major concern when purifving plasma proteins. such as IgG and HSA. Contaminant bacteria can potentially infect a patient receiving the plasma products. or during pasteurisation of the products the bacteria dies releasing dangerous endotoxins. that are harmful to the patient. Bacteria are easily detected by culturing samples on nutrient agar plates.

Aim : To isolate IgG. and HSA. from human plasma spiked with bacteria. using the Gradiflow.

IgG purification procedure Method Platelet free plasma was diluted one part in three with Tris- borate, pH 9.0 running buffer and placed in the upstream of Gradiflow and spiked with E. coli to a concentration of 4x108 cells/ml. A potential of 250V was placed across a separating membrane with a molecular weight cut off of 200kDa (100kDa restriction membranes). A membrane of this size restricts IgG migration whilst allowing smaller molecular weight contaminants to pass through the membrane. leaving IgG and other large molecular weight proteins in the upstream. A second purification phase was carried out using a GABA/Acetic acid buffer, pH 4.6 with a 500kDa cut off separating membrane (3kDa restriction membranes). A potential of 250V reversed polaritv was placed across the system resulting in IgG migration through the membrane leaving other high molecular weight contaminants upstream.

Examination of samples taken at 30 minutes intervals was made on reduced SDS-PAGE 4-25% gels. <BR> <BR> <BR> <P>Bacteria testing<BR> <BR> <BR> <BR> <BR> <BR> <BR> Twenty il of upstream or 100p1 of downstream samples were spread plated onto Luria agar culture plates. The plate were incubated for 24 hours at 37"C. and the number of colonies was counted.

HSAprocedure Vlethod: Pooled normal plasma was diluted one in three with Tris-Borate (TB) running buffer. pH 9.0 and spiked lvith ~4x108 cells/ml of E. coli. The mixture was placed in the upstream of a Gradiflow apparatus. Albumin was isolated from platelet free plasma in a one-phase process using the charge of albumin at a pH above its pI and its molecular weight. Thus a cartridge with a 75kDa cutoff separation membrane was placed between two 50kDa cutoff

restriction membranes. The albumin was removed from high molecular weight contaminants bv its migration through the separation membrane whilst small molecular weight contaminants dissipated through the 50kDa restriction membrane. Samples were taken at regular intervals throughout a 90 minutes run.

The presence of the purified HSA in the downstream was demonstrated bv examination by SDS-PAGE. Bacteria were detected as previouslv described above.

Results of IgG and HSA purification The procedures described successfully purified IgG. and albumin as judged bv electrophoretic examination. The downstream samples containing the purified protein products did not contain detectableE. coli colonies, while the upstream samples produced greatlv in excess of 500 colonies/plate.

CONCLUSION It is possible to purify proteins such as IgG, albumin and fibrinogen from plasma, while simultaneously removing contaminating virus by the methods according to the present invention.

Prion present in plasma can be moved across a 75kDa separation membrane with albumin. however. unlike albumin. the prion is not retained bv the 50kDa restriction membrane. Thus. albumin can be purified from plasma with simultaneous removal of Prion protein.

Evidence has been provided bv the present inventors that it is possible to purifv proteins such as IgG and albumin from plasma, while simultaneouslv removing endotoxin contamination in the starting plasma using the Gradiflow technology.

Furthermore, it has been found that it is also possible to purify proteins such as IgG. and albumin from plasma. while simultaneously removing contaminating bacteria.

It will be appreciated by persons skilled in the art that numerus variations and/or modifications may be made to the invention as shown in the specific embodiments without departing from the spirit or scope of the invention as broadlv described. The present embodiments are. therefore. to be considered in all respects as illustrative and not restrictive.