US20140186819A1 - Liquid to Liquid Biological Particle Concentrator - Google Patents

Abstract

A rapid one-pass liquid filtration system efficiently concentrates biological particles that are suspended in liquid from a dilute feed suspension. A sample concentrate or retentate suspension is retained while eliminating the separated fluid in a separate flow stream. Suspended biological particles include such materials as proteins/toxins, viruses, DNA, and/or bacteria in the size range of approximately 0.001 micron to 20 microns diameter. Concentration of these particles is advantageous for detection of target particles in a dilute suspension, because concentrating them into a small volume makes them easier to detect. Additional concentration stages may be added in “cascade” fashion, in order to concentrate particles below the size cut of each preceding stage remaining in the separated fluid in a concentrated sample suspension. This process can also be used to create a “band-pass” concentration for concentration of a particular target size particle within a narrow range.

Description

• This application is a continuation of U.S. patent application Ser. No. 12/131,015, filed May 30, 2008, now U.S. Pat. No. 8,110,112; which claims priority to U.S. Provisional Patent Application Ser. No. 60/932,271, filed May 30, 2007, and to U.S. Provisional Patent Application Ser. No. 60/961,391, filed Jul. 20, 2007; the contents of which are hereby incorporated by reference herein in their entirety.
BACKGROUND
• 1. Field of Invention
• The invention relates generally to the field of filtration systems. More particularly, the filtration system is used to concentrate dilute materials, such as biological particles, as may be useful in the arts of bioterrorism security, medicine, and environmental science.
• 2. Description of the Related Art
• The difficulties of detecting and quantifying dilute materials in liquids are well known. Existing systems all begin to fail as concentration falls away until, eventually with diminished concentrations of analyte, there is an inability to detect at all. This poses a significant problem to national security where, for example, the postal anthrax attacks of 2001 and the subsequent war on terrorism have revealed shortcomings in the sampling and detection of biothreats. The medical arts are similarly affected by the existing limits on detection, as are the environmental sciences.
• Just because existing systems have inherent detection limits does not mean that it is impossible to study analytes or particles for analysis that fall below these limits. It is possible to concentrate materials for analysis.
• Particle concentration in liquid is traditionally performed using centrifugation. Centripetal force is used for the separation of mixtures according to differences in the density of components that form the mixture. This force separates a mixture forming a pellet of relatively dense material at the bottom of the tube. The remaining solution, which is alternatively called the supernate or supernatant liquid, may then be carefully decanted from the tube without disturbing the precipitate, or withdrawn with a Pasteur pipette. The rate of centrifugation is specified by the acceleration applied to the sample, and is typically measured in revolutions per minute (RPM) or g-forces. The particle settling velocity in centrifugation is a function of particle's size and shape, centrifugal acceleration, the volume fraction of solids present, the density difference between the particle and the liquid, and viscosity.
• Problems with the centrifugation technique limit its applicability. The settling velocity of particles in the range of micron and smaller size particles is quite low and, consequently, centrifugal concentration of these particles takes several minutes to many hours. The actual time varies depending on the volume of the sample, the equipment used, and the skill of the operator. It is also difficult to segregate the particles into size ranges. Many successive centrifugations under carefully controlled circumstances may be used to separate particles into size fractions. In these separations, however, some portion of each sample will contain particles of all size fractions present. This is due to the presence of even the smallest particles in the mixture very near the bottom of the centrifugation vessel or tube at the start of the process.
• Traditional flat filtration methodology is used to capture particles from a liquid onto a flat filter, which is usually supported on the back by a screen or fritted support. Many different methods of filtration exist, but all aim to attain the separation of two or more substances. This is achieved by some form of interaction between the substance or objects to be removed and the filter. The substance that is to pass through the filter must be a fluid, i.e. a liquid or gas. The simplest method of filtration is to pass a solution of a solid and fluid through a porous interface so that the solid is trapped, while the fluid passes through. This principle relies upon the size difference between the particles making up the fluid, and the particles making up the solid. In the laboratory, this if often done using a Buchner funnel with a filter paper that serves as the porous barrier.
• One disadvantage of the physical barrier method of filtration is that the substance being filtered from the fluid will clog the channels through the filter over time. The resistance to flow through the filter becomes greater and greater over time as, for example, a vacuum cleaner bag. Accordingly, methods have been developed to prevent this from happening. Most such methods involve replacing the filter; however, if the filter is needed for a continuous process this need for replacement is highly problematic. Scraping and in-situ cleaning mechanisms may be used, but these can be unnecessarily complex and expensive.
• In one example, bacteria may be removed from water by passing them through a filter supported in a Buchner funnel to trap the bacteria on the flat filter. Aerosol particles containing biological materials can also be trapped in the same way. For analysis, the trapped materials are often re-suspended in a known volume of liquid. This allows back-calculation of the original aerosol concentration. One method validated by the Edgewood Chemical Biological Center uses 47 mm glass-fiber filters to capture reference samples for biological analysis. The bacteria are extracted by soaking the filters overnight in 20 mL of buffered saline solution, then vortexed for 3 minutes to disrupt the filter material completely. Subsamples or aliquots of these suspensions are then provided for analysis by viable culture, PCR or other methods.
• Tangential flow filtration is a variant of traditional filtration. This technique is sometimes called side-stream filtration or cross-flow filtration, and most often uses membrane systems to purify proteins. These systems circulate retentate across the membrane surface, which minimizes the fouling of the membrane. This arrangement provides longer membrane use, resulting in higher overall filtration efficiency. This process has been used in processing cell lysate to clean up the fluid for analysis of particular proteins. Millipore Corporation and Pall manufacture tangential flow filter cassettes that may be purchased on commercial order. Tangential flow systems are also used commercially for particles larger than proteins, and on scales larger than in the micron range.
• The membrane in a tangential flow system may be a hollow fiber filter. These filters are commercially produced by a few companies, most notably Spectrum Laboratories, Inc. Hollow fiber filters may be constructed and arranged in packages intended for respective use in such intended environments of use as laboratories, small scale pharmaceutical production companies, and larger scale water treatment facilities.
• Fluid Analytics, Inc. of Portland, Oreg. has developed a liquid sample concentrator that utilizes tangential flow across a flat filter and a proprietary controlled sonication method to efficiently remove collected particles. The unit has a flow rate of 20 ml/min with a sample volume of up to 20 ml and a concentrated volume of less than about 1 ml. The concentration efficiency is 90%.
• Other technologies for concentration of biological particulate matter exist. Sandia National Laboratories, Massachusetts Institute of Technology and, other organizations have developed microfluidic devices that separate and concentrate particles by dielectrophoresis or electrophoresis. These units use microchannels and electric fields to move or collect particles. Sandia has also developed a system that concentrates particles at the interface between two immiscible liquids. Immunomagnetic particles are commercially available for use in the separation and concentration of bacteria.
• Various methods exist for concentrating organisms in liquids prior to detection. Historically, the most common method is to enrich the sample in nutrient broth and then cultivate an aliquot of the broth on an agar plate. The biggest disadvantage of this method is the time requirement. It normally takes 5 to 7 days before organisms can be enumerated on the plates. Other concentration methods include various filtration based methods, adsorption-elution, immunocapture, flocculation, and centrifugation. It is problematic that to date no automated methods have been developed that can rapidly concentrate a large volume of water into a very small sample volume and do this task efficiently. In fact most of these methods fail in each of these areas, most notably efficiency of concentration, and ease of use.
• A considerable amount of research has been performed using hollow fiber ultrafiltration to concentrate bacteria, viruses, and protozoa from large volumes of water. These methods all use variations of tangential flow or dead end filtration with concentration into water or a water and surfactant solution. Most of the methods described are not automated. Generally these systems are capable of concentrating 10 to 100 L water into 100 to 500 mL of concentrated sample; however, it is further problematic that none of the demonstrated technologies provides concentration into volumes of less than 100 mL. Even this volume is much larger than desired for the best possible detection when the concentrator systems are coupled with downstream detection apparatus. This means that a costly and time-consuming second manual concentration step is required to bring the final sample to the desired volume.
• In bioterrorism defense detection systems an aerosol collector captures particles in the air and concentrates them into a liquid volume in the range of 1.5 ml to 15 ml. A portion of this sample is then transferred directly to a detector which analyzes the liquid and determines if any dangerous aerosols have been collected. Advanced, rapid microbiological detectors used in these systems are only capable of analyzing volumes from around 40 μL to 200 μL of liquid at a time. This volume is about 2% or less of a 10 mL sample from the collector. Any remaining fluid is either archived or dumped to waste.
SUMMARY
• The present disclosure addresses the problem outlined above and advances the art by providing a highly efficient filtration system that can be quickly cleaned for resuspension of concentrated particles for analysis.
• In one aspect, the disclosure herein teaches a method and device for concentrating biological particles that are entrained in a fluid. The concentrator cell or unit may use a single or plural hollow fiber filters, or other membranes in tangential flow devices. The filter may be extracted using a small volume of biologically and analytically compatible foamed wash buffer following the completion of the filtration cycle, in order to extract trapped particles from the filter.
• Foam is as especially preferred medium for use in extracting the trapped particles because it has a relatively greater viscosity o or gel strength than regular liquid, and because is occupies a large volume that diminishes to a small amount of liquid when the foam collapses. The liquid portion of the foamed extraction wash material may be any liquid but is normally water with a buffer and surfactant added. The liquid may be held under pressure of, for example, 50 psi to 800 psi, with a water soluble gas such as carbon dioxide or nitrous oxide. One way to make a fine foam that is a minority of a percentage liquid by volume is to release the pressure and agitate the liquid through a mixing fret. The liquid fizzes to make the foam as the gas is released from solution under the reduced pressure. The foam flows through fluidic pathways extending from a permeate side of the filter, across the filter to a permeate side of the filter. In making this transit, the foam flow down the bore of the past the retentate side of the membrane (or down the bore of the hollow fiber) and out, thus extracting the captured particles. Because the gas in the foam escapes rapidly at atmospheric pressure, it quickly returns to a liquid so that it can be processed further as a liquid almost immediately after being dispensed.
• The liquid extraction wash that is to be foamed may be formulated with a variety of additives. Any conventional buffering system may be used to control pH. Salts may be added, as well as foaming agents, film formers, thinners, thickeners, polymers, surfactants, functionalized particles, microspheres, silica particles, tagging materials, proteins, detergents, and other chemical, fluids, or particles. In one aspect, it is possible to add particles or microspheres or other agents that bind with analytes of interest, mix them with an incoming sample feed, and concentrate this sample feed for delivery to analytical equipment.
• The foam may used to extract any number of enclosed surfaces that are added to the system feed for purposes of capturing particles, bacteria, viruses, protozoa, DNA, RNA, proteins, toxins, immunomagnetic beads, molecular probes, or other particles or molecules. The surfaces can include hollow fiber membranes; flat membranes; microsieves, including polymeric or silicon microsieves; silica surfaces (used to capture DNA in the presence of chaotropic salts such as guanidinium thiocyanate or sodium perchlorate); immunomagnetic beads; or other binding surfaces. The use of hydrophobic membranes for sampling air (as the fluid, as opposed to aqueous samples); then extracting the membrane with the extraction foam.
• Concentrator cells may be deployed in series; where the membrane surface area decreases with each cell. In this way, a very large sample can be processed by passing liquid through a cell with a very large surface area, then extracting with a large amount of foam (so the extraction is efficient), then passing the resultant fluid through a second cell that has much lower surface area than the first cell, that cell is then extracted with a much small amount of foam. So, the final sample volume is very small.
• Vibrational energy, such as megasonic energy, ultrasonic energy, or other vibrations may be applied to the filter while passing the sample therethrough or during extraction of the membrane. This energy improves the fluid throughput rate and the extraction efficiency of the membrane surface.
• It is possible to measure foam in a metered volumetric quantity, but also it is difficult to do. Use of a valve that is controlled with a timer may dispense reproducible volumes of foam by controlling the foam pressure and the valve opening time. Alternatively, a volumetric sample loop may be used, in combination with a multi-position valve, such as a rotary valve, for loading with highly reproducible volumes of foam.
• It can be difficult to push gas across a hollow fiber filter membrane, especially when liquid has reached that membrane. Accordingly, in one aspect the system disclosed herein may selectively apply gas pressure to push foam through the system, especially across the filter. Gas pressure may provide needed energy to break up clogs in the retentate or at other locations in the system. Pressurized gas to store the hollow fiber, membrane, microsieves and/or the entire fluid path under high pressure gas, to act as a biocide, to reduce or stop biofilm build up or growth of organisms on the fiber, membrane, microsieves, or inside the system.
• Two or more concentration cells with membranes of different pore sizes may be deployed in parallel, so that size fractionation can be performed. The use of foam for extraction lets much larger surfaces areas be used, which is very important for reducing blinding of the membranes and for allow highly efficient passage of particles smaller than the membrane pore size.
• Since air does not readily travel through hydrophilic membranes of small pore size, various methods of getting aqueous samples to the hydrophilic membrane surface are disclosed. One technique includes pulling a vacuum on the retentate side of the membrane then allowing the fluid to move into the fiber retentate side. Since the hollow fibers may collapse under excessive pressures, it is also possible to pull a vacuum on the retentate side and permeate side of the membrane at the same time. It is also possible to provide a reservoir that is connected to the retentate side of the membrane, so when fluid is pushed into the fiber under pressure the air is compressed into this reservoir and the fluid moves to the membrane surface. Another option is to connect a hydrophobic membrane to the retentate side of the filter so that air will pass through the hydrophobic membrane until the aqueous fluid reaches the membrane.
• Foam may be used for similar applications, such as extracting particles or molecules from other surfaces, then pulling the resultant liquid off of the surface with a squeegee and vacuum wand. That sample can then be concentrated with the concentrator.
• Since the concentrator cell may be enclosed, it is capable of holding particles, bacteria, viruses, protozoa, DNA, RNA, proteins, toxins, immunomagnetic beads, molecular probes, microspheres or other particles or molecules in place on the membrane surface without extracting these particle with foam. The carrier fluid is removed then sample can be washed, tagged, or treated in other ways by pulling various wash buffers, EDTA, ethanol, lysis buffers, denaturing buffers, tagging solutions, immunomagnetic beads, immunobeads, silica beads, nanomaterials, or other liquids or particles.
• In one aspect, these advantages may be obtained by using specially constructed concentrator cells that employ hollow fiber filters to concentrate samples for analysis. A foam extraction of trapped particles is particularly advantageous. The cell bodies are constructed with various ports that are operated in a specific sequence of events to trap particles of interest and then extract them using a foam extraction technique to provide a concentrated sample for analysis.
• In one aspect, a novel one pass tangential flow filtration system offers significant advantages over previous methods of biological particulate matter concentration. This system concentrates the collected sample prior to analysis. The liquid volume of the sample is quickly reduced. As compared to centrifugation, which typically takes from 0 to 30 minutes to concentrate micron-sized particles, this process can be accomplished in 5 to 60 seconds for a 10 mL initial volume.
• Unlike typical single-pass flat filtration, the sample remains in liquid form for transport and analysis. The detection limit for the target agent is lowered, with respect to the media originally sampled. The final sample volume is advantageously reduced much further than in previously known methods, while kept in liquid form, allowing detection in devices such as multi-well plate readers that utilize small input samples. The reduced-size samples can be more efficiently stored and transported by microfluidic handling methods. The device may be constructed to separate particles in one pass into different size fractions for analysis for certain agents. For example, cells and spores may be concentrated separately from viruses and biological toxins. Further, the size range that is concentrated can be narrow, or “band-pass” to concentrate a small size range fraction from a complex matrix, such as an environmental sample. The device may be used to reduce the onboard fluid storage capacity of aerosol samplers, by recycling the cleaned liquid back to the collection cycle after the sampled particles are removed into a small volume for analysis.
• The instrumentalities disclosed herein are more readily adapted to automated systems than other technologies including centrifugation, flat filtration, and other methods. The flow-through nature of the device allows for straightforward configuration into an automated detection system.
• The disclosed instrumentalities may be used in conjunction with biological collection/sampling systems where the resulting sample is contained in a liquid. Alternatively, the device could be coupled with a detection device that receives liquid samples. For many of these sampling and detection systems, it is advantageous to concentrate the sample prior to analysis, for reasons that are described below. In the field of medicine, in particular pathology, samples taken from patients may have a low concentration of an organism, virus, or toxin that causes illness, which must be identified in order to effect treatment. Concentration of such medical samples prior to analysis is also advantageous, for reasons that are described below. In the field of environmental science, field samples taken in the course of biological studies or investigations may contain biological materials of interest in low concentrations. Concentration of such materials is advantageous, for reasons that are described below. Additionally, for the three fields of interest described here, the device can be of further use in that by using a staged arrangement, concentrated samples may be separated by size if desired, without sacrificing concentration ability or efficiency. For the bioterrorism security field, a further advantage is the reduction in consumables (sampling fluid) that can be afforded by recycling the filtered permeate. Further, this concentration system is compatible with test particles, such as the Biological Particulate Matter Analogue, U.S. Pat. No. 7,179,596 (Page, Alburty, Brown, Huebner, 2007), a DNA-tagged polystyrene microsphere packaged in a metered dose aerosol dispenser and marketed by Sceptor Industries, Inc., as the “BioSim” for safely testing biological aerosol collection/detection systems.
• The foregoing instrumentalities have significant utility in medical, environmental, or security applications. For example, concentration in the manner described facilitates aerosol sampling for pathogens or bioterrorism threat agents that can withstand being placed in a liquid sample for analysis. A list of such pathogens may be provided, for example, as recognized by the Centers for Disease Control. These organisms may be studied using conventional techniques that are facilitated by the concentration of samples as described above:
List 1: CDC Category A and B Bioterrorism Agents List
• Category A (Definition Below)
• • Anthrax (Bacillus anthracis)
  • Botulism (Clostridium botulinumtoxin)
  • Plague (Yersinia pestis)
  • Smallpox (variola major)
  • Tularemia (Francisella tularensis)
  • Viral hemorrhagic fevers (filoviruses [e.g., Ebola, Marburg] and arena viruses [e.g., Lassa, Machupo])
• Category B (Definition Below)
• • Brucellosis (Brucellaspecies)
  • Epsilon toxin ofClostridium perfringens
  • Food safety threats (e.g.,Salmonellaspecies,Escherichia coliO157.H7,Shigella)
  • Glanders (Burkholderia mallei)
  • Melioidosis (Burkholderia pseudomallei)
  • Psittacosis (Chlamydia psittaci)
  • Q fever (Coxiella burnetii)
  • Ricin toxin fromRicinus communis(castor beans)
  • Staphylococcal enterotoxin B
  • Typhus fever (Rickettsia prowazekii)
  • Viral encephalitis (alphaviruses [e.g., Venezuelan equine encephalitis, eastern equine encephalitis, western equine encephalitis])
  • Water safety threats (e.g.,Vibrio cholerae, Cryptosporidium parvum)
List 2: Secondary Potential Biological Threat Agents
• Viri/Prions
• • Flaviviruses (Yellow fever virus, West Nile virus, Dengue, Japanese Encephalitis, TBE, etc.)
  • Hep A, B, C
  • Prions (CJD, BSE, CWD)
  • Alphaviruses (VEE, EEE, WEE)
  • Nipah virus
  • Rabies virus
  • Rhinovirus (could be modified?)
  • Polioviruses
  • Hantaviruses
  • Filoviruses (Ebola, Marburg, Lassa)
• Bacilli
• • Mycobacterium tuberculosis, drug resistant
  • Mycobacteriaother than TB, likeC. leprae
  • Streptococcus pneumoniae
  • S. pyogenes
  • S. aureus
  • Clostridium tetani
  • C. difficile
  • Bacillus cereus
  • Coxiella brunette(Q fever)
  • Francisella tularensis
  • Borrelia recurrentis
  • Rickettsia rickettsii
  • R. prowazekii
  • Shigella sonnei
  • Bartonella henselae
  • Yersinia enterolitica
  • Y. pseudotuberculosis
  • Neisseria meningitidis
  • Legionella pneumophila
  • Burkfholderia pseudomallei
  • Pasturella multocida
• Other Pathogenic Microorganisms
• • Cryptosporidium parvum
  • Histoplasma capsulatum
  • Cryptococcus neoformans
  • Aspergillus niger
• Pathogenic Fungi
• • Acremomiumspp.
  • Alternaria alternate
  • Apophysomyces elegans
  • Aspergillus terreus
  • Bipolarisspp.
  • Bipolaris spicifera
  • Blastoschizomyces capitatus
  • Candida krusei
  • Candida lusitaniae
  • Cladophialophora bantiana
  • Cunnihamella berholletiae
  • Curvularia lunata
  • Exserohilum rostratum
  • Fusarium moniliforme
  • Fusarium solani
  • Hansenula anomala
  • Lasiodilodia theobromae
  • Malassezia furfur
  • Paecilomyces lilacinus
  • Paecilomyces bariotii
  • Penicillium mameffei
  • Phialemonium curvatura
  • Philophora parasitica
  • P. richardsiae
  • Ramichloridiumspp.
  • Rhizomucor pusillus
  • Rhizopus rhizopodiformus
  • Rhodotorula rubra
  • Sacchromyces cerevisiae
  • Scedosporium prolificans
  • Trichosporon beigelii(T. asahii)
  • Wangiella dermatitidis
Physical Sizes of Some Agents and Surrogates:Target:
• • Bacillus thuringiensisendospore—approximately 1 μm
  • Bacillus anthracisendospore—approximately 1 μm
  • Yersinia pestis—Gram negative rod-ovoid 0.5-0.8 μm in width and 1-3 μm length
  • Yersiniarohdei—approximately 1 μm
  • Venezuelan Equine Encephalitis—70 nm (0.07 μm)
  • Gamma-killed MS2—2 mD or about 25 nm (0.025 μm) (but will pass through a 300 kD pore size but is retained by a 100 kD pore size Wick and McCubbin—ECBC)
  • Ovalbumin—45 kD or 6 nm (0.006 μm)
  • Botulinum Toxoid A—150 to 900 kD or 10 nm to 70 nm (0.01 μm to 0.07 μm) (Normally published as 150 kD however some publications state that toxoid A can be released as complexes comprised of the 150 kD toxin protein along with associated non-toxin proteins and can therefore be released in 900 kD, 500 kD, and 300 kD forms.
  • DNA—1000 Bp or 600 kD up to 15,000 Bp or 9 mD
• In other aspects, after concentration, detection of the threat agent(s) may be performed on nucleic acids that have been isolated as described above and amplified by conventional polymerase chain reaction (PCR) or PCR-like methods.
• Detection or study of the agent(s) of interest may be performed by conventional immunoassay methods, or by ultraviolet light fluorescence methods.
• Even if a threat agent is present, it is potentially useful to know that concentration and analysis resulting in a non-detect result can provide assurance that if the target agent is present, it is present in such a low quantity that the resulting risk to the affected population is minimal.
• Separation of the sample into desirable size fractions may advantageously concentrate the target particles into separate but equally concentrated size fractions for analysis by different detection methods listed above, such as in separating and concentrating particles larger than 0.2 microns to segregate generally bacteria from other pathogens. A small size range or “band-pass” may be separated out and concentrated for interrogation for a particular threat agent or surrogate, such as by separating and concentrating particles from 0.2 microns diameter to 2 microns diameter to segregate most bacterial spores and concentrate them separately from smaller and larger particles present in the initial sample. It is also possible to separate and concentrate particles from 0.005 microns to 0.2 microns in diameter to separate most viruses and concentrate them separately from smaller and larger particles present in the initial sample. Actual test examples include viral equine encephalitis, or VEE; 0.06 microns in diameter.
• Another mode of concentration may to separate and concentrate particles from 0.001 microns (approximately 5 kiloDaltons) to 0.01 microns (approximately 100 kiloDaltons) to separate toxins and proteins and concentrate them separately from smaller and larger particles present in the initial sample.
• In other aspects, the above types of sampling and analysis are advantageously performed for the fields of homeland security, corporate security, and military force protection are useful when preceding work by automated sampling and analysis systems, such as those developed for government programs Portal Shield, Joint Programs Biological Detection System (JPBDS), US Postal Service Biological Detection System (BDS), and systems under development, such as the Biological Aerosol Networked Detection (BAND) system and Rapid Aerosol Biological Identification System (RABIS).
• In other aspects, it is possible to test samples resulting from manual swabbing of surfaces onto wetted swabs, pads, or pieces of filter material, are often taken for bioterrorism security monitoring and typically extracted into a volume of liquid resulting in a 2 to 20 mL volume initial sample. Samples like these may be quickly concentrated to much smaller volumes in the range of 4-400 uL.
• In still other aspects, samples my be concentrated for water sampling in search of bioterrorism agents, or in the interest of public health and safety, especially where a sample may contain target agent(s) that are thought to be a threat to the health of humans, animals or plants, causing societal disruption and economic harm. Agricultural products and livestock environments may also be studied by the instrumentalities herein disclosed.
• Additional fields of use include medical research and diagnostics. For example, sample concentration is useful in cancer research where very low concentrations of experimental drugs in body fluids or urine are the targets of analysis, and in allergy diagnosis where low quantities of specific antigens are the targets of analysis in body fluids. Health effects research may also benefit by determining health effects known to be caused by various materials in inhaled particulate matter with aerodynamic diameter below 2.5 microns (PM 2.5). Benefit is seen in the field of forensic medicine where low concentrations of toxins or venoms are the targets of analysis in body fluids. Other aspects of use may include the study of operating rooms for surface extraction and air monitoring of pathogens, as well as pharmaceutical manufacturing where the biological aerosol particulate matter concentration is regulated by the United States Food and Drug Administration.
• In other aspects, environmental studies may benefit to include any types of sampling and analysis that are performed for the field of environmental study, such as in assessing health effects through research regarding various materials in inhaled particulate matter with aerodynamic diameter below 2.5 microns (PM 2.5) or high altitude aerosol research where low quantities of particulate are collected and must be concentrated for study. These instrumentalities may benefit cleanrooms where very low aerosol concentrations of aerosol particles are collected for monitoring that is aimed at source control.
• Commercially available hollow fiber filter tubes are arranged in the device such that the dilute feed suspension is fed under pressure in a single pass into one end of the tubes, while excess cleaned water is removed under vacuum from a space surrounding the tubes. The working pressure is the differential pressure between the feed pressure and the cleaned liquid side of the filters. This arrangement accelerates the process compared to the use of pressure only on the feed and recycling the retentate several times, as is done normally (for example, Millipore Corporation'sPellicon 3 System for concentrating monoclonal antibodies, Spectrum Laboratories KrosFlo Research II System). An air bleed valve on the retentate side is opened at the start of the filtration process to bleed out air from the inside of the filter. Bleeding this air is essential to fast initiation of the filtration cycle when using a hydrophilic filter as air will not pass through a hydrophilic membrane of small pore size. Balancing the pressure appropriately by providing gas pressure on the permeate side of the filter during the extraction process improves extraction efficiency.
• To further improve the efficiency of the concentration device, a biocompatible surfactant such as Triton X-100 is added to the feed at low levels, such as 0.1-0.01% by volume. This liquid is an insignificant volumetric addition, but can increase the efficiency of concentration from the 40% to 65% range to nearly 100%. Buffered surfactant solutions such as 0.1% tris buffered saline (TBS) or phosphate buffered saline (PBS) with 0.01 to 0.1% Triton or Tween are commonly used in the collection fluids of bioaerosol samplers.
• Mechanical shear such as produced by a shaker motor, or an ultrasonic or megasonic horn is also used to improve throughput efficiency and processing speed.
• Hollow fiber filters made of different materials are used for application specific reasons. Such fibers are commonly made of mixed cellulose esters (ME), polyethersulfone (PES), polysulfone (PS), polypropylene (PP) polyacrylonitrile (PAN) and hydrophilic polydivinylidene fluoride (PVDF) and other materials such as stainless steel and ceramics. Various advantages and disadvantages accrue to each type of filter. Some design criteria are size of pores, biocompatibility, smoothness, fouling potential, and physical strength.
• Cleaning and decontamination of hollow fiber filters is desirable when the device is used to concentrate multiple samples. Cleaning and decontamination of PES filters, such as the ones used in the devices ofEmbodiments 1 and 2 can be performed using 3% hydrogen peroxide or 0.5% sodium hypochlorite (10% dilution of commercially available bleach). PS and PES filters can also be autoclaved and steam-cleaned. Cleaning of these filters cannot be performed using ethyl acetate (typically used to dissolve polystyrene microspheres used for performance testing) or acetone, which dissolves PES. PES-compatible solvents include water, carbonated water, methanol, ethanol, hexane, and ether. Triton X-100 surfactant is compatible with the PES hollow fiber filters.
• Sample extraction may be performed into a small volume using foam made from the extraction surfactant. This procedure cleans the concentrator, while simultaneously enhancing extraction efficiency and allowing for greatly reduced retentate volumes. A small volume of liquid may be used to create a large volume of foam. Since the boundaries of the bubbles present in the foam must remain intact to remain as foam, the boundaries of the bubbles at the interface of the filter and the extraction foam must always be touching. As the foam proceeds through the hollow fiber filter, it sweeps the concentrate through the device. When the foam is extracted from the device and collapses, the remaining product is a small volume of liquid. This volume will normally be in a range of less than 5 microliters to 1 milliliter, but may be up to 100 milliliter or more for use in extraction of large filter surface areas. In its simplest form, the foam may be made in a separate container, then injected to sweep the sample from the concentrator into the sample collection port. However, the use of a sample loop to measure the amount of liquid used to make the foam is preferred in order to generate samples of consistent size. In addition to surfactant foams that are generated by mixing air and a surfactant solution, foam may also be generated with a carbonated surfactant solution. Following carbonation, the solution is agitated by dispensing through an orifice, frit, filter, or capillary tube. The Triton foam extraction methods described here can also be used for extraction and cleaning of other collection surfaces in aerosol samplers and collectors. The use of foam to extract these surfaces can provide a significant increase in extraction efficiency and significant decrease in final sample volume.
BRIEF DESCRIPTION OF THE DRAWINGS
• FIG. 1 shows a three dimensional perspective view of a concentrator cell according to a first embodiment;
• FIG. 2 shows a right side elevational view of the concentrator cell shown inFIG. 1;
• FIG. 3 shows a midsectional view of the concentrator cell taken alongline2A-2A′ ofFIG. 2;
• FIG. 4 shows a three dimensional perspective view of a concentrator cell according to a second embodiment;
• FIG. 5 shows a right side elevational view of the concentrator cell shown inFIG. 4;
• FIG. 6 shows a midsectional view of the concentrator cell taken alongline5B-5B″ ofFIG. 5;
• FIG. 7 shows a three dimensional perspective view of a concentrator cell according to a third embodiment;
• FIG. 8 shows a right side elevational view of the concentrator cell shown inFIG. 7;
• FIG. 9 shows a midsectional view of the concentrator cell taken along line8C-8C′ ofFIG. 8;
• FIG. 10 shows a three dimensional perspective view of a concentrator cell according to a fourth embodiment;
• FIG. 11 shows a right side elevational view of the concentrator cell shown inFIG. 10;
• FIG. 12 shows a midsectional view of the concentrator cell taken alongline11D-11D′ ofFIG. 11;
• FIG. 13 shows a three dimensional perspective view of a concentrator cell according to a fifth embodiment;
• FIG. 14 shows a right side elevational view of the concentrator cell shown inFIG. 13;
• FIG. 15 shows a midsectional view of the concentrator cell taken alongline14E-14E′ ofFIG. 14;
• FIG. 16 shows a three dimensional perspective view of a concentrator cell according to a sixth embodiment;
• FIG. 17 shows a right side elevational view of the concentrator cell shown inFIG. 16;
• FIG. 18 shows a midsectional view of the concentrator cell taken alongline17F-17F′ ofFIG. 17;
• FIG. 19 shows a three dimensional perspective view of a concentrator cell according to a seventh embodiment;
• FIG. 20 shows a right side elevational view of the concentrator cell shown inFIG. 19;
• FIG. 21 shows a midsectional view of the concentrator cell taken alongline20G-20G′ ofFIG. 20;
• FIG. 22 shows a three dimensional perspective view of a concentrator cell according to an eighth embodiment;
• FIG. 23 shows a right side elevational view of the concentrator cell shown inFIG. 22;
• FIG. 24 shows a midsectional view of the concentrator cell taken alongline23H-23H′ ofFIG. 23;
• FIG. 25 shows a three dimensional perspective view of a concentrator cell according to a ninth embodiment;
• FIG. 26 shows a right side elevational view of the concentrator cell shown inFIG. 25;
• FIG. 27 shows a midsectional view of the concentrator cell taken along line26I26I′ ofFIG. 26;
• FIG. 28 shows a three dimensional perspective view of a concentrator cell according to a tenth embodiment;
• FIG. 29 shows a right side elevational view of the concentrator cell shown inFIG. 28;
• FIG. 30 shows a midsectional view of the concentrator cell taken alongline29J-29J′ ofFIG. 29;
• FIG. 31 shows a three dimensional perspective view of a concentrator cell according to an alternate embodiment with respect to that shown inFIG. 28;
• FIG. 32 shows a right side elevational view of the concentrator cell shown inFIG. 31;
• FIG. 33 shows a front elevational view of the concentrator cell shown in
• FIG. 31;
• FIG. 34 shows a three dimensional perspective view of a concentrator cell according to an eleventh embodiment;
• FIG. 35 shows a right side elevational view of the concentrator cell shown inFIG. 34;
• FIG. 36 shows a midsectional view of the concentrator cell taken alongline35K-35K′ ofFIG. 35;
• FIG. 37 shows a three dimensional perspective view of a concentrator cell according to a twelfth embodiment;
• FIG. 38 shows a right side elevational view of the concentrator cell shown inFIG. 37;
• FIG. 39 shows a midsectional view of the concentrator cell taken along line37L-37L′ ofFIG. 38;
• FIG. 40 shows an automated concentration system, which is depicted in a schematic layout wherein any of the foregoing concentrator cells may be used;
• FIG. 41 shows an automated concentration system, which is depicted in a schematic layout wherein any of the foregoing concentrator cells may be used;
• FIG. 41A provides expanded detail with respect to a feature ofFIG. 41;
• FIG. 42 shows an extraction foam generator according to a first embodiment, as depicted in a three dimensional perspective view;
• FIG. 43 shows a right side elevational view of the extraction foam generator shown inFIG. 42;
• FIG. 44 shows a midsectional view of the extraction foam generator taken alongline43N-43N′ ofFIG. 43;
• FIG. 45 shows an extraction foam generator according to a second embodiment, as depicted in a three dimensional perspective view in combination with the concentrator cell shown inFIG. 13;
• FIG. 46 shows a right side elevational view of the extraction foam generator shown inFIG. 45;
• FIG. 46A provides additional detail with respect to a feature ofFIG. 45;
• FIG. 47 shows an extraction foam generator according to a third embodiment, as depicted in a three dimensional perspective view;
• FIG. 48 shows a right side elevational view of the extraction foam generator shown inFIG. 47; and
• FIG. 49 shows a midsectional view of the extraction foam generator taken alongline48P-48P′ ofFIG. 48.
DETAILED DESCRIPTION
• There will now be shown and described one or more concentrator cells that are provided with a tangential flow media which may be used to concentrate biological particles and subsequently extracted with foam to obtain, for example, concentrated proteins, microorganisms, and/or nucleic acids.
• FIGS. 1,2 and3 shows aconcentrator cell100 that may be constructed from a rectangular block of plastic or metal that is drilled to create various fluid channels. Barbed fittings are glued in place for tubing connections to formports102,104,106,108. Flexible tubing (not depicted) may be attached to the ports102-108, and pinch clamps or valves (also not depicted) may be used to control flow through this tubing. These structures function as valves or flow control mechanism which are understood to be present in proximity to each fluidic port in this disclosure for operation according to the functionality described therewith, whether or not the flow control device is actually depicted A potting material, such asglue110,112, holds ahollow fiber filter114 in place. As used herein, the term “potting material” means a destructible or removable material that is used to anchor a hollow fiber filter, and which may be removed for renewal of the filter.FIG. 3 shows the internal fluid channels together with respective arrows indicating the direction of fluid flow in each ofports102,104,106,108. The respective ports include an extraction fluidflush port102,permeate port104, feedport106, andretentate port108.
• Concentrator cell100 operates as follows. Theretentate port108 and extraction fluidflush port102 are closed at the start of the sample concentration process. A vacuum is optionally applied at thepermeate port104, and the feed is introduced under pressure at thefeed port106. The sample then passes through thehollow fiber filter114. When the entire feed sample has passed through the hollow fiber filter the pressure and vacuum are equalized betweenports104,106, then thefeed port106 is closed. A vacuum is applied to theretentate port108 and theflush port102 is opened allowing a small, pre-measured volume of surfactant liquid or foam to flush the captured particles off of the inside surface of the hollow fiber filter, producing the desired final volume of concentrated fluid.
• FIGS. 4,5 and6 show aconcentrator cell400.Cell400 resemblescell100; however, two hollow fiber filters402 are used instead of one, and anintegrated reservoir404 retains a predetermined volume of the feed sample which is used to flush thefibers402 at the end of the concentration cycle.Potting material406,408 retains the hollow fiber filters402 in place.FIG. 6 shows the internal fluidic pathways together with arrows indicating flow direction at each of theretentate port410, feedport412, is thepurge port413, and permeateport414.
• Concentrator cell400 operates as follows. Theretentate port410 is closed and thepurge port413 is opened. Feed is injected under pressure through thefeed port412 until thereservoir404 is full, then thepurge port413 is closed. A vacuum is applied to thepermeate port414 and pressure is applied to thefeed port412. Once the feed sample has been completely injected, the pressures are equalized atports412,414, then thefeed port412 is closed and theretentate port410 is opened with vacuum there being applied. Thepurge port413 is opened and the feed remaining in thereservoir404 is used to flush the captured particles off of the inside surface of the hollow fiber filters402, producing the desired final volume of concentrated fluid.
• FIGS. 7,8 and9 show a third embodiment indicated as concentrator cell700. Concentrator cell700 is similar to that ofconcentrator cell100. As shown inFIG. 9, distal portion702 of a hollow fiber filter704 is potted in a barbed insert706 mounted in a retentate port708. This arrangement advantageously minimizes dead volume in the retentate port708 for improved sample concentration. A permeate purge port710 is added to facilitate the removal of the permeate fluid that is trapped around the outside of the fiber at the end of the feed cycle.FIG. 9 shows internal pathways of fluidic communication through the concentrator cell700 with arrows indicating flow direction at each of the retentate port708, feed port712, permeate port710, extraction fluid port714, and permeate purge port716. Potting material718 retains the hollow fiber filter704 in place.
• Concentrator cell700 operates as follows. The retentate port708 is opened and the feed is injected through the feed port712 to purge air from inside the hollow fiber filter704. The retentate port708 is then closed and pressure is applied to the feed port712 as a vacuum is applied to the permeate port710. Once the feed has all been injected, the feed pressure is equalized across ports708,710, and the permeate purge port716 is opened. Thus, remaining permeate fluid is pulled through the permeate port710 while the permeate pressure is equalized. The retentate port708 is next opened and a pre-measured volume of extraction fluid is injected under pressure through the extraction fluid port714 to flush the captured particles off of the inside surface of the hollow fiber filter704, producing the desired final volume of concentrated fluid.
• FIGS. 10,11 and12 show yet another embodiment indicated asconcentrator cell1000.Concentrator cell1000 is similar to that of concentrator cell700, but has acentral opening1002 fitted with aflexible tube1004 that may be removed to facilitate easier replacement of ahollow fiber filter1006.FIG. 12 shows the internal flow pathways withinconcentrator cell1000 together with arrows indicating flow direction at each offeed port1006,extraction fluid port1008, permeate purgeport1010,permeate port1012, andretentate port1014.Potting materials1016,1018 retain thehollow fiber filter1004.
• Operation ofconcentrator cell1000 proceeds as in the case of concentrator cell700. Theretentate port1014 is opened and a feed is injected through thefeed port1006 to purge air from inside thehollow fiber filter1004. Theretentate port1014 is then closed and pressure is applied to the feed as a vacuum is applied to thepermeate port1012. Once the feed has all been injected, the feed pressure is equalized acrossports1006,1014. Thepermeate purge port1010 is opened and remaining permeate fluid is pulled through thepermeate port1012 while the permeate pressure is equalized. Then, theretentate port1014 is opened and a pre-measured volume of extraction fluid is injected under pressure through theextraction fluid port1008 to flush the captured particles off of the inside surface of thehollow fiber filter1004, producing the desired final volume of concentrated fluid.
• FIGS. 13,14, and15show concentrator cell1300, which has additional features with respect to previous embodiments.Concentrator cell1300 includes integrated feed, extraction fluid, air bleed, and retentate valves, and an integrated foam extraction fluid generator. The potting holes are drilled in the plane perpendicular to the fluid channels to decrease their length and make the cell more compact. The removable center tube introduced inembodiment 4 is also used. This is the first cell which utilizes surfactant foam for the extraction fluid, which greatly increases extraction efficiency and decreases the final concentrated sample volume.FIG. 15 shows each component ofconcentrator cell1300 with arrows indicating the direction of fluid flow in each port. The ports includefeed port1302, permeate purgeport1304,permeate port1306, andretentate port1308. An elongateshiftable feed valve1310 controls flow throughpassageway1312. An elongate shiftableextraction fluid valve1314 controls flow throughpassageway1316. An elongate shiftableair bleed valve1318 controlspassageway1320, while an elongateshiftable retentate valve1322 controlspassageway1324.Potting materials1326,1328 are advantageously disposed in parallel to the flow direction throughhollow fiber filter1330, thus decreasing the length of the potting materials and eliminating the necessity of drilling additional holes to receive the potting materials. Aremovable tube1332 facilitates replacement of thehollow fiber filter1330.Feature1338 indicates anextraction foam generator1340 that is described in additional detail below.
• Concentrator cell1300 operates as follows. Thefeed valve1310 and theair bleed valve1318 are opened, and the feed fluid is slowly fed into thefeed port1302. Air in thehollow fiber filter1330 is forced out, and when the feed fluid reaches the bottom of thehollow fiber filter1330 theair bleed valve1318 is closed. Vacuum is then applied to thepermeate port1306, and the feed fluid is forced through thehollow fiber filter1330. When the feed fluid has been pushed completely through, thepermeate purge port1304 is opened to flush the liquid around the outside of thehollow fiber filter1330 out thepermeate port1304. The pressure on the hollow fiber filter is then equalized between thefeed port1302 and permeateport1306, then thefeed valve1310 is closed. Then, theretentate valve1322 and theextraction fluid valve1314 are opened. Theextraction foam generator1340 is then used to flush the captured particles off of the inside surface of thehollow fiber filter1330 until the desired final volume of concentrated fluid is reached.
• FIGS. 16,17, and18 introduce the concept of a ‘cascade’ or ‘band pass’system1600 allowing for concentration and separation of different target particle size ranges. Also, high pressure liquid chromatography (HPLC) style compression fittings are used to make the port connections which are more durable and can withstand higher pressures than barbed connectors.FIG. 18 shows each component with arrows indicating the direction of fluid flow in each ofextraction foam port1802, feed Aport1804, feedB port1806, permeate purge Aport1808, permeate purgeB port1810, is thepermeate A port1820,permeate B port1822,retentate A port1824,retentate B port1826. Each of these ports is provided with a HPLC-style compression fitting, for example, as fitting1827 (seeFIG. 18). Elongate shiftable valves control flow through associated fluidic pathways including extractionfoam A valve1828, extractionfoam B valve1830, feed Avalve1832, feedB valve1834,retentate A valve1836,retentate B valve1838. Filters includehollow fiber filter1840 andhollow fiber filter1842.
• In this “band pass” configuration, hollowfiber filter A1840 captures particles over a certain size, for example two micron, and passes smaller particles entrained with the remaining fluid into thepermeate A port1820.Feed B port1806 is fluidically connected to permeate Aport1820. Hollowfiber filter B1842 captures all of the particles that hollowfiber filter A1840 passes into thepermeate A port1820. In this example,system1600 operates according to the principles described above; however, everything below a predetermined size cutoff, such as particles of two microns or less or even particle-free fluid, passes through thepermeate B port1822.
• FIGS. 19,20 and21 show aconcentrator cell1900 that is designed to facilitate starting a concentration cycle when the hollow fiber filter is wet and there is gas in the system. Hydrophilic fibers allow water based solutions to pass through them easily; however, gas can not pass through the wet fiber due to the capillary action of the water in the fiber pores. This essentially causes the fiber to lock up until the gas is purged from the inside of the fiber. This problem was addressed in previous embodiments by opening the retentate valve until the feed solution forced all of the gas out of the fiber; however, this is problematic for systems that are automated under a system of electronic controls. This embodiment introduces the use of a short hydrophobic fiber inline with the main hydrophilic fiber. The hydrophobic fiber allows gas to flow through it but not liquid, so the gas is effectively purged from the fiber automatically.
• Another new feature of this embodiment is a gas injection port which allows any extraction foam left in the fiber to be forced out through the retentate port without adding to the final extracted liquid volume. Furthermore, from this design forward the concentration process includes pressurizing the permeate side of the hollow fiber filter with gas while the extraction foam is being injected. This prevents the extraction foam from pushing through the fiber and into the permeate.
• FIG. 21 shows each component ofconcentrator cell1900 where arrows indicate the direction of fluid flow in each ofretentate port1902,permeate port1904, permeate purgeport1906, feedport1908,extraction foam port1910, andgas injection port1912.Valves1914,1916, and1918 are one-way check valves permitting flow in the directions indicated.Potting material1920,1922 retains ahollow fiber filter1924.HPLC compression fittings1926,1927 allow quick removal and replacement of thehollow fiber filter1924 mounted also withinhollow tube1928.Potting material1930,1932 seals channels connecting the hydrophobic and hydrophilic fiber permeate sides. A hydrophobic fiber is located downstream ofhollow fiber filter1924.
• Concentrator cell1900 operates as follows. Theretentate valve1902 is closed and a vacuum is applied to thepermeate port1904. This forces feed solution into thefeed port1908. Any gas trapped in the feed side of thehollow fiber filter1924 is forced out through thehydrophobic fiber1934. Once the feed solution has all passed through thehydrophilic fiber1924, thepermeate purge port1906 is opened and the pressure is equalized across the surface of the fibers. Then, gas pressure is applied through thepermeate port1904, and theretentate port1902 is opened. A predetermined volume of extraction foam is injected under pressure through theextraction foam port1910 to flush the captured particles off of the inside surface of thehollow fiber filter1924. Finally, gas is forced through thegas injection port1912, which forces any remaining foam out of thehollow fiber filter1924, producing the desired final volume of concentrated fluid.
• FIGS. 22,23 and24 show an embodiment identified asconcentrator cell2200, which is a compact design for use where size of the concentrator cell is an issue.Concentrator cell2200 contains, for example, ahollow fiber filter2202 that is less than one inch long.FIG. 24 shows each component ofconcentrator cell2200 with arrows indicating the direction of fluid flow in each ofretentate port2204,permeate port2206, feedport2208,extraction foam port2210,gas injection port2212, and permeatepurge port2214.Potting material2216 retains hollow fiber filter2218.
• Concentrator cell2200 operates as follows. Theretentate valve2204 is opened and a vacuum is applied to thepermeate port2206. The feed solution is injected through thefeed port2208 until the feed solution reaches the end of thehollow fiber filter2202. Then theretentate port2204 is closed. When the feed solution has all been forced through thehollow fiber filter2202, thepermeate purge port2214 is opened to remove the remaining fluid around thehollow fiber filter2204 and equalize the pressure across the fiber surface. Gas pressure is next applied through thepermeate port2206. Theretentate port2204 is opened, and extraction foam is injected through theextraction foam port2210 to flush the captured particles off of the inside surface of thehollow fiber filter2202. Finally, gas is forced through thegas injection port2212, which forces any remaining foam out of thehollow fiber filter2202, producing the desired final volume of concentrated fluid.
• FIGS. 25,26 and27 show an embodiment according toconcentrator cell2500 which, by way of example, combines the hydrophobic fiber section for gas removal fromconcentrator cell1900 with the small size ofconcentrator cell2200. The main changes from previous embodiments are the lack of a gas injection port, and the feed port has been relocated to the bottom of the cell. The feed port was moved to help ease the clearing of clogs in the fiber.Concentrator cell2500 may also contain ahollow fiber filter2502 that is less than one inch long.FIG. 27 shows each component ofconcentrator cell2500 with arrows indicating the direction of fluid flow in each ofretentate port2504,permeate port2506, permeate purgeport2508,extraction foam port2510, and feedport2512.Valves2516,2518 are one-way check valves.Numerals2520,2522,2504 indicate potting material. A hydrophilichollow fiber filter2526 assists with the purging of internal gas under system automated control, as is described above.
• Concentrator cell2500 operates as follows. Theretentate port2504 is closed and a vacuum is applied to thepermeate port2506. Feed solution is forced into thefeed port2512. Any gas trapped in the feed side of thehollow fiber filter2502 is forced out through thehydrophobic fiber2526. Once the feed solution has all passed through thehydrophilic fiber2526, thepenneate purge port2508 is opened and the pressure is equalized across the surface of the fibers. Then, gas pressure is applied through thepermeate port2506, and theretentate valve2504 is opened. A predetermined volume of extraction foam is injected under pressure through theextraction foam port2510 to flush the captured particles off of the inside surface of the hollow fiber filter, producing the desired final volume of concentrated fluid.
• FIGS. 28,29, and30show concentrator cell2800 according to another embodiment.Concentrator cell2800 is very similar toconcentrator cell2200 except, by way of example,concentrator cell2800 is made up of modular components that allow different length fibers to be used in the same cell by changing the tube between the respective upper andlower manifolds2802,2804.
• FIG. 30 shows each component ofconcentrator cell2800 where arrows indicate the direction of fluid flow in each ofretentate port2806,permeate port2808,purge port2810, feedport2812,extraction foam port2814, andgas injection port2816.Valves2818,2820, and2822 are one-way check valves.Potting material2824,2826 retainshollow fiber filter2828, as does ahollow tube2830 and compression fitting. Amodular bar2834 may be provided in various lengths to adjust the assembly for selected lengths ofhollow fiber filter2828, and this modular bar may be secured withfasteners2836,2838.
• Concentrator cell2800 operates as follows.Retentate valve2806 is opened and a vacuum is applied to thepermeate port2808. Feed solution is injected through thefeed port2812 until the feed solution reaches the end of thehollow fiber filter2828. Then theretentate port2806 is closed. When the feed solution has all been forced through thehollow fiber filter2828, thepermeate purge valve2810 is opened to remove the remaining fluid around thehollow fiber filter2828 and equalize the pressure across the fiber surface. Gas pressure is next applied through thepermeate port2808, and theretentate valve2806 is opened. A predetermined volume of extraction foam is injected through theextraction foam port2814 to flush the captured particles off of the inside surface of thehollow fiber filter2828. Finally, gas is forced through thegas injection port2820, which forces any remaining foam out of the fiber and produces the desired final volume of concentrated fluid.
• FIGS. 31,32 and33 show theconcentrator cell2800 in an alternate configuration where there is a loopedfiber3100. This configuration allows long fibers to be used without greatly increasing the size of the concentrator cell.
• FIGS. 34,35, and36 show an embodiment according toconcentrator cell3400, which is designed for long, large diameter hollow fiber filters.
• FIG. 36 shows each component ofconcentrator cell3400 where arrows indicate the direction of flow through each ofretentate port3402, feedport3404,permeate port3406, permeate purgeport3408,gas injection port3410, andextraction foam port3412.Valves3414,3416 and3418 are one-way check valves.Potting material3420,3422 retainshollow fiber filter3424 and forms fluid channels.
• Concentrator cell3400 operates as followsretentate valve3402 is opened and a vacuum is applied to thepermeate port3406. The feed solution is injected through thefeed port3404 until it reaches thepotting material3424, then theretentate valve3402 is closed and the feed pressure is increased. The feed solution forces the gas in thehollow fiber filter3424 to compress and fill the channel above the fiber while the feed solution is being forced through thehollow fiber filter3424. When all of the feed solution has been forced through, thepermeate purge port3408 is opened, and the remaining fluid outside thehollow fiber filter3424 is flushed into thepermeate port3406 while the pressure equalizes across the surface of thehollow fiber filter3424. Then, gas pressure is applied through thepermeate port3406, and theretentate valve3402 is opened. A predetermined volume of extraction foam is injected through theextraction foam port3412 to flush the captured particles off of the inside surface of thehollow fiber filter3424. Finally, gas is forced through thegas injection port3410. This forces any remaining foam out of the fiber, producing the desired final volume of concentrated fluid.
• FIGS. 37,38 and39show concentrator cell3700 which, by way of example. Combines a hydrophobic fiber section with the modular design ofconcentrator cell2800.FIG. 39 shows each component ofconcentrator cell3700 where arrows indicate the direction of fluid flow in each ofretentate port3702, feedport3704,permeate port3706, permeate purgeport3708,extraction foam port3710, andgas injection port3712.Valves3714,3716,3718 are one-way check valves.Potting materials3720,3722 retain hydrophobic hollow fiber filter whilehollow fiber filter3726 is retained bycompression fittings3728,3730 andsheath3732.Tube3728 connects the permeate channels of the twofibers3723,3726.
• Concentrator cell operates as follows.Retentate valve3702 is closed and a vacuum is applied to thepermeate port3706. Feed solution is forced into thefeed port3704. Any gas trapped in the feed side of the fiber is forced out through thehydrophobic fiber3723. Once the feed solution has all passed through thehydrophilic fiber3726, thepermeate purge3708 is opened flushing the remaining fluid around the outside of the fiber into thepermeate port3706, and the pressure is equalized across the surface of the fibers. Then, gas pressure is applied through thepenneate port3706, and theretentate valve3702 is opened. A predetermined volume of extraction foam is injected under pressure through theextraction foam port3710 to flush the captured particles off of the inside surface of thehollow fiber filter3726. Finally, gas is forced through thegas injection port3710, which forces any remaining foam out of the fiber, producing the desired final volume of concentrated fluid.
• FIG. 40 is a schematic diagram showing anautomated system4000 that may be adapted to incorporate any of the foregoingconcentrator cells100,400,700,1000,1300,1600,1900,2200,2500,2800,3400, or3700. In particular as shown,system4000 incorporatesconcentrator cell2800 as described above, together with as well as the extraction foam generator ofFIGS. 47-49 below. Carbon dioxide gas as the injection gas. InFIG. 40, like numbering of identical elements is retained with respect toFIG. 30, except a prime “′” is added to designate inclusion of these same elements insystem4000 through communicative fluidic pathways insystem4000.System4000 additionally includes various elements under automated system control. A system controller is shown generally ascontroller4001 and may route control signals to the various elements ofsystem4000 by circuitry or wireless transmission according to programmable instructions.
• Elements ofsystem4000 under automated controls include afeed pump4002, anextraction foam valve4004,gas injection valve4006, permeatepurge valve4008,permeate pump4010, andretentate pump4012.
• In the intended environment of use, thefeed port2812′ is connected to a reservoir (not shown) which is filled with the feed solution. Thepermeate purge port2810′ is connected to a filter (not shown) in ambient air. Thepermeate port2808′ is dumped to another reservoir (not shown) with the opening above the fluid level so air can be pulled back into theline4014 if thepermeate pump4010 is reversed. Theretentate port2806′ is dumped into a sample container (not shown) for analysis. Thegas injection port2816′ is connected to a regulated carbon dioxide gas cylinder (not shown). Theextraction foam port2814′ is connected to the foam generator (not shown).
• System4000 operates as follows under automated control. Theextraction valve4004,gas injection valve4006, and permeatepurge valve4008, are all closed while theretentate valve4012 is opened. The feed solution is poured into the sample reservoir and thefeed pump4002 starts to pump the solution into the cell2600′. Once the feed solution reaches the bottom of thehollow fiber filter2828′, theretentate valve4012 is closed, and thepermeate pump4010 starts to pull a vacuum on the permeate side of thehollow fiber filter2828′. When the feed solution has been completely forced through thehollow fiber filter2828′, thefeed pump4002 reverses slowly to relieve the pressure on the feed side of thehollow fiber filter2828′, and thepermeate purge valve4008 is opened, allowing ambient air to be pulled through thepermeate purge port2810′ to flush the permeate fluid out thepermeate port2810′. Then thepermeate purge valve4008 is closed and thepermeate pump4010 is reversed, pressurizing the permeate side of thehollow fiber filter2828′ with air. Theretentate valve4012 is next opened, and then theextraction foam valve4004 is opened for a timed period allowing a predetermined volume of extraction foam to enter the concentrator cell to flush the captured particles off of the inside surface of thehollow fiber filter2828′. Thegas injection valve4006 is opened, flushing any remaining foam out theretentate port2806′.
• FIG. 41 shows asystem4100 that is designed pressure extraction and high pressure cell storage. When aconcentrator cell4102 is not in use, thesystem4100 may pressurize thesample cell4102 with high pressure gas or high pressure extraction foam to inhibit bacterial growth.System4100 uses a sample loop, rather than a timed valve, to meter the extraction foam. This allows for higher pressures to be used and more precise control of the final extracted volume. To address the problem of gas on the feed side of ahollow fiber filter4104, a vacuum is applied to the inside of the fiber to remove any gas before the feed solution is pumped.
• System4100 contains a plurality of components where arrows indicate the direction of fluid movement through elements including highpressure gas port4106, sample loop overflow (waste)port4108,extraction foam port4110, permeate purgeport4112,permeate port4114, feedport4116, feeddrain port4118, andretentate port4120.
• Elements ofsystem4100 under automated control may includegas metering valve4122 that precedes a high pressure gas oneway check valve4124 downstream from highpressure gas port4106. A four-position gas valve4126 may distribute gas throughsystem4100. There are provided a sampleloop metering valve4128, asample loop4130, cellfoam storage valve4132, extraction foam oneway check valve4134, cell foamstorage metering valve4136, theextraction foam valve4138, and permeatepurge valve4140.Potting materials4142,4144 retain thehollow fiber filter4104. Pumps include thepermeate pump4146 and thefeed pump4148.Numeral4150 designates the permeate valve, while numeral4152 designates the retentate valve which is the same type of a four position valve as isvalve4126.
• In the intended environment of use, the highpressure gas port4106 is connected to a regulated gas source (not shown). The sampleloop overflow port4108 is connected to a waste container (not shown). Theextraction foam port4110 is connected to a foam generator (not shown). Thepenneate purge port4112 is also connected to the waste container; however it is connected in such a way that when thepermeate pump4146 is pulling vacuum on thecell4102, ambient air can enter theport4112. Thepermeate port4112 is connected to the permeate reservoir (not shown), however it is connected in such a way that when thepermeate pump4146 is pressurizing thecell4102, ambient air can enter theport4112. Thefeed port4116 is connected to the feed reservoir (not shown). Thefeed drain port4118 is connected to the waste container. Theretentate port4120 is dumped into a sample container (not shown) for analysis.
• System4100 uses HPLC style rotary selection valves.FIG. 41A shows the port labels for the valves, the valve is shown in position AB. When a valve of this type is said to be turned off, it is rotated to the nearest position between ports, preventing any fluid movement. All of the four-way valves in thissystem4100 have the same port labels.
• Thegas metering valve4122, the sampleloop metering valve4128, and the cell foamstorage metering valve4136 all perform a similar purpose. These valves are used to slow the fluid flow and maintain a high fluid pressure on one side. Shown are adjustable needle valves, however, calibrated orifices could be used in place of needle valves.
• The concentration and sample recovery cycle is performed as follows. All valves are initially off. Theextraction foam valve4138 is rotated to position CD, connecting the feed and permeate sides of thehollow fiber filter4104. Thepermeate valve4150 is then opened and thepermeate pump4146 pulls a vacuum on thecell4102. This removes any gas on the feed side of thehollow fiber filter4104. Once a vacuum has been created on the feed side of thehollow fiber filter4104, theextraction foam valve4138 is turned off and theretentate valve4152 is rotated to position AD. Thefeed pump4148 starts forcing the feed solution through thehollow fiber filter4104. While the feed solution is being forced through thehollow fiber filter4104, thegas valve4126 is rotated to position AB, and thesample loop4130 is pressurized with high pressure gas. This keeps the extraction foam in liquid form while it is filling the sample loop. Once thesample loop4130 has been pressurized, theextraction foam valve4138 rotates to position AB and thegas valve4126 rotates to position BC. Liquid extraction foam slowly forces out the gas in thesample loop4130 while the pressure is maintained by the sampleloop metering valve4128. Once thesample loop4130 has been completely filled with liquid extraction foam, both thegas valve4126 and theextraction foam valve4138 are turned off. When all of the feed solution has been forced through thehollow fiber filter4104, thepermeate purge valve4140 is opened to flush out the remaining permeate from around the outside of thehollow fiber filter4104, and thefeed pump4148 is reversed until the pressure across the surface of thehollow fiber filter4104 is equalized. Then, thepermeate purge valve4140 is closed and thepermeate pump4146 is reversed to pressurize the permeate side of thehollow fiber filter4104. Theretentate valve4152 is now rotated to position AB. Then, theextraction foam valve4138 is rotated to position BC and the extraction fluid expands into foam as it enters thehollow fiber filter4104. This scrubs the captured particles off of the inside surface of the fiber and flushes them out theretentate port4120.Gas valve4126 is rotated to position AB. Gas flushes the remaining extraction foam out of thesample loop4130 and through the fiber; producing the desired final volume of concentrated fluid. Finally, all valves are turned off.
• When theconcentrator cell4102 is not being used, it may be stored in a high pressure gas environment to inhibit bacterial growth. The high pressure gas storage of the cell is performed as follows: All valves are initially off. Theextraction foam valve4138 is rotated to position CD to connect the feed and permeate sides of thehollow fiber filter4104. This allows both sides of thehollow fiber filter4104 to be pressurized evenly, and prevents the fiber from rupturing or collapsing. Now, thegas valve4126 is rotated to position AD, and gas slowly pressurizes the cell. Once the desired pressure is reached, thegas valve4126 is turned off. To return the cell to a low pressure state, thegas valve4126 is rotated to position CD, and the gas is allowed to slowly escape.
• When theconcentrator cell4102 will not be used for an extended period of time, it is preferred for it to be stored in a liquid environment. The high pressure foam storage of the cell is performed as follows. All valves are initially off. First, theextraction foam valve4138 is rotated to position CD to connect the feed and permeate sides of thehollow fiber filter4104. This allows both sides of thehollow fiber filter4104 to be pressurized evenly, and prevents the fiber from rupturing or collapsing. Then, thepermeate valve4150 is opened and thepermeate pump4146 pulls a vacuum on thecell4102 to remove any gas. Once the gas has been removed, thepermeate pump4146 is turned off and thepermeate valve4150 is closed. Now, the cellfoam storage valve4132 is opened and extraction fluid is slowly forced into thecell4102. The extraction fluid initially expands into foam, however as the pressure increases it collapses back into a liquid. Once the desired pressure is reached, the cell foam storage valve is turned off. To return the cell to a low pressure state, thegas valve4126 is rotated to position CD and the extraction fluid is allowed to slowly escape. Once the pressure is low enough, thepermeate valve4150 is opened and thepermeate pump4146 pulls a vacuum on thecell4102 to remove the remaining extraction foam.
• FIGS. 42,43 and44 show one embodiment of anextraction foam generator4200 that may be used to make foam for the extraction purposes discussed above. Foam is created by adding a high pressure gas to a water based solution. In most cases, a surfactant is used in the solution to generate thicker and dryer foam.
• FIG. 44 shows each component of the extraction foam generator with arrows indicating the direction of fluid flow in each ofgas port4202,extraction foam port4204, and is theliquid port4206. A mixingfrit4208 combines feed from thegas port4202 andliquid port4206, ideally to form a solution where the gas is dissolved in the liquid, for foaming discharge at eventual reduced pressure throughextraction foam port4204. Foam is formed in this manner by flashing the gas from the liquid at reduced pressure. Longevity of the foam may be controlled by selecting the type and amount of a particular surfactant.
• Extraction foam generator4200 operates as follows. Gas is injected into thegas port4202, and a metered amount of liquid extraction solution is injected into theliquid port4206. The gas and liquid mix in thefrit4208 with the mixture being discharged throughextraction foam port4204. Foam is generated by reducing the pressure on the effluent, or by the mixing action of frit4208 alone if the pressure at frit4208 is insufficient to dissolve the gas in the liquid which flows out theextraction foam port4204.
• FIGS. 45 and 46 show another embodiment according toextraction foam generator4500, which is designed to be integrated directly into a concentrator cell (see, e.g.,detail1338 ofFIG. 15).FIG. 46 shows theconcentrator cell1300 as previously described.FIG. 46A provides additional detail with respect to theextraction foam generator4500.
• FIG. 46A shows each component of theextraction foam generator4500 with arrows indicating the direction of fluid flow in each ofgas port4502,liquid port4504, andfoam port4506. Ahollow fiber filter4508 may be used as a mixing frit, as sealed by pottingmaterial4510,4512. Foam production is assisted by the action of mixingchamber4512.
• Extraction foam generator4500 operates as follows. A predetermined volume of liquid extraction solution is injected into theliquid port4502. High pressure gas is next injected through thegas port4504 and through thehollow fiber filter4508. As the gas enters themixing chamber4512, the agitation of the liquid generates foam which expands and exists through thefoam port4506.
• FIGS. 47,48 and49 show yet another embodiment according to extractionfoam generator system4700.System4700 uses a pressure chamber to force high pressure gas to dissolve into a liquid extraction fluid solution. As long as the extraction fluid is under pressure it remains a liquid, however, if the pressure is reduced it expands into foam.
• FIG. 49 shows each component ofsystem4700 with arrows indicating the direction of fluid flow throughgas port4702, extraction foam port4704,liquid fill port4706 and purgeport4708. Foam production is assisted by the action of mixingfrit4710.Wall4712 defines achamber4714.Tube4716 communicates withpressure chamber4714 to provide a liquid level indicator and may be translucent for this purpose.
• System4700 operates as follows. The pressure in thechamber4714 is released through thepurge port4708 and thechamber4714 is filled with liquid extraction solution throughliquid port4706. Once the pressure chamber is full, the liquid fill port (5) and the purge port (6) are closed off. High pressure gas is injected through thegas port4702 and through the mixingfrit4710. The gas dissolves into the liquid at the design pressure for operation ofchamber4714, but when the compressed fluid is introduced to a low pressure environment, either before or after discharge through extraction foam port4704, the gas expands and generates foam.
WORKING EXAMPLES
• Performance testing of the device as shown inFIG. 1 above was conducted using carboxylate-coated yellow-green fluorescent polystyrene microspheres (Polysciences, Inc., Warrington, Pa.). Three sizes of microspheres were used; 1 micron, 3 micron, and 4.5 micron diameter. For each test run, 10 mL of a diluted microsphere suspension in water was used as feed. The results of nine 1-micron tests, eight 3-micron tests, and nine 4.5-micron tests were averaged, and the results are summarized graphically inFIG. 5. Note that these tests were performed without surfactant or shear added to the process, and the efficiency ranged from approximately 40% to 65%. Testing of the device was then performed with the addition of 0.01% Triton X-100 surfactant, improving the efficiency of the device to nearly 100%. Efficiency improvement data are shown in Table 1 below.

• TABLE 1
  Efficiency Improvement using Surfactant
  Condition number 16: 3 um carboxylate-coated YG microspheres
  Cell efficiency improvement test; 0.01% Triton X-100 Surfactant added

  	Feed	Ret.
  	vol	Vol	Concentration	Volume	Cell
  Sub run #	(mL)	(mL)	factor	reduction%	efficiency %

  1	10.0	0.235	43.5	97.7	102
  2	10.0	0.157	50.6	98.4	79
  3	10.0	0.255	39.3	97.4	101
  4	10.0	0.274	39.3	97.3	108
  5	10.0	0.189	52.5	98.1	99
  6	10.0	0.254	42.1	97.5	107
  7	10.0	0.228	48.1	97.7	109
  Condition			45.1		100.7
  average:

Biological Particle Concentration Data
• The device shown inFIG. 4 was used to process a set of nine 10 mL samples ofBacillus subtilisspores suspended in phosphate buffered saline solution containing 0.01% Triton X-100 surfactant. The average concentration factor was 65% x with an average efficiency of 59%. These data are summarized in Table 2.

• TABLE 2
  Biological Particle Enrichment and Throughput Efficiency

  	Sample	Enrichment		final concentrate vol.
  	number	factor	Efficiency	(mL)

  	1	70	64%	0.093
  	2	99	92%	0.1362
  	3	68	63%	0.2276
  	4	58	53%	0.1236
  	5	46	42%	0.1053
  	6	63	58%	0.1544
  	7	41	38%	0.129
  	8	63	58%	0.1401
  	9	70	65%	0.1295
  	Average	65	59%	0.1387

Foam Concentration Data
• One test was conducted using 4.5 micron diameter carboxylate coated yellow-green fluorescent polystyrene microspheres, which were concentrated using the device ofFIG. 1 combined with the foam generating attachment described inFIG. 42. The 10 mL samples were reduced to a final volume of 13 microliters with a concentration factor of 688× and the volume reduction was 99.87% with an efficiency of 89.2%.

• TABLE 3
  Foam extraction efficiency at various foam concentrations

  		Feed	Sample			Sample	Sample		Volume
  Test	Feed	vol	vial	Sample + vial	Dilution	average	Vol	Concentration	reduction	Concentration
  no.	(FIU)	(mL)	tare (g)	(g)	factor	(FIU)	(mL)	factor	(%)	efficiency (%)

  A	1066	10.0	1.972	2.001	0.010	2384	0.030	229	99.705	67.6
  B	1066	10.0	1.979	2.000	0.007	2362	0.021	317	99.789	66.8
  C	1066	10.0	1.966	1.975	0.003	3056	0.009	991	99.913	86.0
  D	1066	10.0	1.977	1.982	0.002	2639	0.005	1518	99.951	74.2
  The dilution factor is calculated as the sample weight in grams/3 grams added fluid + sample weight in grams, as the concentrated sample must be diluted for analysis.

• A set of test runs was conducted using bacterial endospores (Bacillus atrophaeus, ATCC 6633, MedTox, Inc.). which were concentrated using the device ofFIG. 7, combined with the foam generating attachment described inFIG. 42. The 10 mL samples were reduced to an average final volume of 271 microliters with a concentration factor of 63× with an efficiency of 53%. The consistency of performance in the extraction volumes was improved by partially automating the extraction cell. An Omron electronic timer was used in conjunction with a solenoid valve and trigger button to control foam injection times to within 0.001 second. For these experiments, the timer was set to 0.020 seconds for the first 3 extractions, and to 1.020 seconds for the final rinse (extraction 4). The solenoid valve was modified to reduce the interior dead volume by potting a length of Teflon tubing into it for attachment to the concentration cell. The fiber filter used was 0.5 mm ID ME with 0.2 micron pore size, approximately 10 cm long.

• TABLE 4
  Bacterial spore concentration assessments

  			Volume			Total	Total
  Condition	Ret. Vol	Concentration	reduction	Efficiency	Total conc.	extract	efficiency
  number 34	(mL)	factor	(%)	(%)	factor	vol (mL)	(%)

  Run A - Feed	0.094
  Run A - extract 1	0.083	25.62	99.175	21.143
  Run A - extract 2	0.089	2.21	99.111	1.970
  Run A - extract 3	0.093	1.51	99.072	1.400	29.3	0.264	24.5
  Run A - Rinse	0.472	0.64	95.278	3.042
  Run B - Feed	0.102
  Run B - extract 1	0.083	3.49	99.169	2.899
  Run B - extract 2	0.104	0.89	98.963	0.921
  Run B - extract 3	0.095	0.68	99.050	0.645	5.1	0.282	4.46
  Run C - Rinse	0.391	0.37	96.094	1.439
  Run C - Feed	0.218
  Run C - extract 1	0.086	37.13	99.139	31.971
  Run C - extract 2	0.104	2.24	98.965	2.316
  Run C - extract 3	0.100	1.82	99.001	1.817	41.2	0.290	36.1
  Run C - Rinse	0.409	0.81	95.910	3.308
  Run D - Feed	0.101
  Run D - extract 1	0.079	45.00	99.205	35.774
  Run D - extract 2	0.102	2.87	98.981	2.927
  Run D - extract 3	0.096	1.75	99.043	1.670	49.6	0.277	40.4
  Run D - Rinse	0.479	0.63	95.215	3.013
  Run E - Feed	0.100		98.997
  Run E - extract 1	0.083	129.84	99.172	107.504
  Run E - extract 2	0.101	8.77	98.993	8.830
  Run E - extract 3	0.097	1.96	99.032	1.900	140.6	0.280	118
  Run E - Rinse	0.384	0.62	96.158	2.397
  Run F - Feed	0.099		99.009
  Run F - extract 1	0.080	108.01	99.203	86.082
  Run F - extract 2	0.094	4.35	99.059	4.093
  Run F - extract 3	0.061	2.19	99.389	1.336	114.5	0.235	91.5
  Run F - Rinse	0.288	0.87	97.118	2.493
  				Average:	63	0.271	53
  				Std. Dev.:	53	0.020	43

• Concentration efficiency of the device shown inFIG. 1 was investigated using carboxylate, a functionally coated biosimulant, on polystyrene microspheres. The efficiencies shown in Table 5, below, are for concentrating 1.5 mL of fluid into 100 μL; this produces concentration factors ranging from 9× to 14×. The processing time was less than 90 seconds.

• TABLE 5
  Concentration efficiency at various particle sizes

  Particle Size (μm)	Represented Particle	Efficiency

  4.5	Agglomerates of bacteria	95%
  1.0	Single bacteria	85%
  0.05	Viruses	75%
  0.025	DNA, Lower limit-viruses	60%

• It will be appreciated that the foregoing instrumentalities teach by way of example, and not by limitation. Accordingly, those skilled in the art understand that the invention is not limited to what is strictly disclosed, but also pertains to what is understood by those skilled in the art on the basis of the teachings herein. The inventors hereby state their intention to rely, as may be needed, upon the Doctrine of Equivalents to protect the fullness of their rights in what is claimed.

Claims (20)

1. A method for concentrating a sample of biological particulates, the method comprising:

flowing a predetermined amount of a foam wash from a permeate side of a hollow fiber filter across the hollow fiber filter to a feed side of the hollow fiber filter such that an amount of biological particulates on the feed side of the hollow fiber filter becomes concentrated in the foam wash, resulting in a desired amount of a concentration of biological particulates; and

collecting the desired amount for analysis of the biological particulates.

2. The method inclaim 1, comprising flowing a process feed material that bears particulates entrained in a fluid through the hollow fiber filter to separate the amount of biological particulates from the fluid by trapping the amount of biological particulates on the feed side of the hollow fiber filter.

3. The method inclaim 2, further comprising pulling a vacuum on the permeate side of the hollow fiber filter to pull the process feed material through the hollow fiber filter.

4. The method inclaim 1, wherein a pressurized wash liquid and water-soluble gas mixture is released from under pressure and agitated to create the foam wash, the method further comprising controlling the pressure of the mixture.

5. The method inclaim 1, further comprising opening a valve that is controlled with a timer to dispense the foam wash.

6. The method inclaim 5, further comprising controlling a valve opening time.

7. A device for concentrating a sample of biological particulates, the device comprising:

a wash reservoir adapted to connect to a permeate side of a hollow fiber filter, the wash reservoir containing a wash liquid and a water soluble gas under pressure resulting in a predetermined amount of a foam wash; and

a rotary valve adapted to release the predetermined amount of the foam wash from the permeate side of the hollow fiber filter across the hollow fiber filter to a feed side of the hollow fiber filter to generate a desired amount of a concentration of biological particulates within the foam wash;

a feed reservoir connected to the feed side of the hollow fiber filter, the feed reservoir containing a process feed material that bears the amount of biological particulates entrained in a fluid;

a means for flowing the process feed material through the hollow fiber filter to separate the amount of biological particulates from the fluid by trapping the amount of particulates on the feed side of the hollow fiber filter;

wherein the concentration of biological particulates is collected for analysis.

8. (canceled)

9. The device inclaim 7, further comprising a hollow fiber cell containing the hollow fiber filter.

10. (canceled)

11. (canceled)

12. The device inclaim 7, wherein the foam wash is biologically and analytically compatible with the biological particulates.

13. The device inclaim 7, further comprising a timer controlling release of the valve.

14. (canceled)

15. The device inclaim 7, wherein the wash liquid includes at least one of a buffer, a salt, a foaming agent, a film former, a polymeric material, a surfactant, a microsphere, a silica particle, a tagging material, a protein, or a detergent.

16. A method for concentrating a sample of biological particulates, the method comprising:

releasing a wash liquid and water-soluble gas mixture from under pressure, the release creating a predetermined amount of a foam wash from the mixture, from a permeate side of a hollow fiber filter across the hollow fiber filter to a feed side of the hollow fiber filter which contains an amount of biological particulates; and

collecting a desired amount of a concentrate of biological particulates in the foam wash for analysis.

17. The method inclaim 16, further comprising agitating the mixture during release.

18. The method inclaim 16, further comprising applying vibration to the mixture during release.

19. The method inclaim 16, further comprising pushing the foam wash across the hollow fiber filter using pressurized gas.

20. The method inclaim 16, further comprising inhibiting microbial growth by storing the hollow fiber filter under high pressure.

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