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Publication numberUS20040121454 A1
Publication typeApplication
Application numberUS 10/633,448
Publication dateJun 24, 2004
Filing dateAug 1, 2003
Priority dateMar 10, 2000
Also published asCA2400978A1, CN1441703A, EP1265708A1, EP1265708A4, US7485454, US20090275115, WO2001068257A1
Publication number10633448, 633448, US 2004/0121454 A1, US 2004/121454 A1, US 20040121454 A1, US 20040121454A1, US 2004121454 A1, US 2004121454A1, US-A1-20040121454, US-A1-2004121454, US2004/0121454A1, US2004/121454A1, US20040121454 A1, US20040121454A1, US2004121454 A1, US2004121454A1
InventorsAndrey Jury, Mark Angelino
Original AssigneeBioprocessors Corp.
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
US 20040121454 A1
Chemical and biological reactors, including microreactors, are provided. Exemplary reactors include a plurality of reactors operable in parallel, where each reactor has a small volume and, together, the reactors produce a large volume of product. Reaction systems can include mixing chambers, heating/dispersion units, reaction chambers, and separation units. Components of the reactors can be readily formed from a variety of materials. For example, they can be etched from silicon. Components are connectable to and separable from each other to form a variety of types of reactors, and the reactors can be attachable to and separable from each other to add significant flexibility in parallel and/or series reactor operation.
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What is claimed is:
1. A chemical or biochemical reactor comprising:
a reaction unit including a chamber having a volume of less than 1 ml, an inlet to the chamber connectable to a source of a chemical or biological starting material, and an outlet of the chamber for release of a product of a chemical or biological reaction involving the starting material; and
a collection chamber connectable to the outlet of the reaction chamber, the collection chamber having a volume of greater than 1 liter.
  • [0001]
    This application claims the benefit of priority under 35 U.S.C. 120 to U.S. patent application Ser. No. 09/707,852, filed Nov. 7, 2000, which application claims the benefit of priority under 35 U.S.C. 119(e) of U.S. Provisional Patent Application Serial No. 60/188,275, filed Mar. 10, 2000. These applications are incorporated herein by reference.
  • [0002]
    The present invention relates generally to chemical or biochemical microreactors, and more particularly to a microreactor for the production of the product of a chemical or biochemical reaction, including a plurality of individuated microreactors constructed to operate in parallel.
  • [0003]
    A wide variety of reaction systems are known for the production of the product of chemical or biochemical reactions. Chemical plants involving catalysis, biochemical fermenters, pharmaceutical production plants, and a host of other systems are well-known.
  • [0004]
    Systems for housing chemical and biochemical reactions not necessarily for the production of product also are known. For example, continuous-flow systems for the detection of various analytes in bodily fluids including blood, such as oxygen, glucose, and the like are well known.
  • [0005]
    In many of these and other systems, the capacity of the system (the volume of material that the system is designed to produce, process, or analyze) is adjusted in accordance with the volume of reactant, product, or analyte desirably processed or analyzed. For example, in large-scale chemical or pharmaceutical production, reactors are generally made as large as possible to generate as large a volume of product as possible. Conversely, in many areas of clinical diagnosis, where it is desirable to obtain as much information as possible from as small a physiological sample as possible (e.g., from a tiny drop of blood), it is a goal to minimize the size of reaction chambers of sensors. Several examples of small-scale reactor systems, including those used in clinical diagnoses and other applications, follow.
  • [0006]
    U.S. Pat. No. 5,387,329 (Foos, et al.; Feb. 7, 1995) describes an extended use planar clinical sensor for sensing oxygen levels in a blood sample.
  • [0007]
    U.S. Pat. No. 5,985,119 (Zanzucchi, et al.; Nov. 16, 1999) describes small reaction cells for performing synthetic processes in a liquid distribution system. A variety of chemical reactions including catabolic, anabolic reactions, oxidation, reduction, DNA synthesis, etc. are described.
  • [0008]
    U.S. Pat. No. 5,674,742 (Northrup, et al.; Oct. 7, 1997) describes an integrated microfabricated instrument for manipulation, reaction, and detection of microliter to picoliter samples. The system purported by is suitable for biochemical reactions, particularly DNA-based reactions such as the polymerase chain reaction.
  • [0009]
    U.S. Pat. No. 5,993,750 (Ghosh, et al.; Nov. 30, 1999) describes an integrated micro-ceramic chemical plant having a unitary ceramic body formed from multiple ceramic layers in the green state which are sintered together defining a mixing chamber, passages for delivering and reacting fluids, and means for delivering mixed chemicals to exit from the device.
  • [0010]
    Biochemical processing typically involve the use of a live microorganism (cells) to produce a substance of interest. Biochemical and biomedical processing account for about 50% of the total drug, protein and raw amino-acid production worldwide. Approximately 90% of the research and development (R&D) budget in pharmaceutical industries is currently spent in biotechnology areas.
  • [0011]
    Currently bioreactors (fermentors) have several significant operational limitations. The most important being maximum reactor size which is linked to aeration properties, to nutrient distribution, and to heat transfer properties. During the progression of fermentation, the growth rate for cells accelerates, and the measures required to supply the necessary nutrients and oxygen sets physical and mechanical constraints on the vessel within which the cells are contained. Powerful and costly drives are needed to compensate for inefficient mixing and low mass-transfer rates. Additionally, as metabolism of cells accelerates, the cells generate increased heat which needs to be dissipated from the broth.
  • [0012]
    The heat transfer characteristics of the broth and the vessel (including heat exchanger) impose serious constraints on the reaction scale possible (see Table 1). While the particular heat load and power requirements are specific to the reaction, the scale of reaction generally approaches limitations at ˜10 m3 as in the case of E. coli fermentation (Table 1). The amount of heat to be dissipated becomes excessive due to limits on heat transfer coefficients of the broth and vessel. Consequently, the system of vessel and broth will rise in temperature. Unfortunately, biological compounds often have a relatively low upper limit on temperature for which to survive (<45 C. for many). Additionally, power consumption to disperse nutrients and oxygen and coolant requirements to control temperature make the process economically unfeasible (see Table 1).
    TABLE 1
    Oxygen- and Heat- Transfer Requirements
    for E. coli: Effects of Scale
    (mmol/ Volumea Pressure Power Heat Load Coolantb
    L h) (m3) (psig) (hp) (Btu/h) ( F.)
    150 1 15 5.0   84 000 40
    200 1 25 4.9  107 000 40
    300 1 35 7.1  161 000 40
    400 1 35 6.9  208 000 40
    150 10 15 50.2  884 000 40
    200 10 25 50.0 1 078 000 40
    300 10 35 75.7 1 621 000 22
    400 10 35 77.0 2 096 000 5
  • [0013]
    Aside from reactor scalability, the design of conventional fermentors has other drawbacks. Due to the batch and semi-batch nature of the process, product throughput is low. Also, the complexity and coupled nature of the reaction parameters, as well as the requirement of narrow ranges for these parameters, makes control of the system difficult. Internal to the system, heterogeneity in nutrient and oxygen distribution due to mixing dynamics creates pockets in the broth characterized by insufficient nutrients or oxygen resulting in cell death. Finally, agitation used to produce as homogeneous a solution as possible (typically involving impellar string to simultaneously mix both cells and feeds of oxygen and nutrients) causes high strains which can fracture cell membranes and cause denaturation.
  • [0014]
    While a wide variety of useful reactors for a variety of chemical and biological reactions, on a variety of size scales exist, a need exists in the art for improved reactors. In particular, there is a current need to significantly improve the design of bioreactors especially as the pharmaceutical and biomedical industries shift increasingly towards bioprocessing.
  • [0015]
    The present invention provides systems, methods, and reactors associated with small-scale chemical or biochemical reactions.
  • [0016]
    In one aspect the invention provides a chemical or biochemical reactor. The reactor includes a reaction unit including a chamber having a volume of less than one milliliter. The chamber includes an inlet connectable to a source of a chemical or biological starting material and an outlet for release of a product of a chemical or biological reaction involving the starting material. A collection chamber is connectable to the outlet of the reaction chamber. The collection chamber has a volume of greater than one liter.
  • [0017]
    In another aspect the invention involves a chemical or biochemical reactor system. The system includes a mixing chamber including a plurality of inlets connectable to a plurality of sources of chemical or biochemical reagents, and an outlet. A reaction chamber is connectable to and removable from the mixing chamber, and has a volume of less than one milliliter. The reaction chamber includes an inlet connectable to and removable from the outlet of the mixing chamber, and an outlet for release of a product of a chemical or biological reaction involving the starting material.
  • [0018]
    In another aspect the invention provides methods. One method includes carrying out a chemical or biological reaction in a plurality of reaction chambers operable in parallel, where each reaction chamber has a volume of less than one milliliter. Product of the reaction is discharged from the plurality of reaction chambers simultaneously into a collection chamber having a volume of greater than one liter.
  • [0019]
    Other advantages, novel features, and objects of the invention will become apparent from the following detailed description of the invention when considered in conjunction with the accompanying drawings, which are schematic and which are not intended to be drawn to scale. In the figures, each identical or nearly identical component that is illustrated in various figures is represented by a single numeral. For purposes of clarity, not every component is labeled in every figure, nor is every component of each embodiment of the invention shown where illustration is not necessary to allow those of ordinary skill in the art to understand the invention.
  • [0020]
    [0020]FIG. 1 illustrates a microbioreactor of the invention including mixing, heating/dispersion, reaction, and separation units, in expanded view;
  • [0021]
    [0021]FIG. 2 illustrates the system of FIG. 1 as assembled;
  • [0022]
    [0022]FIG. 3 illustrates the mixing unit of the system of FIG. 1;
  • [0023]
    [0023]FIG. 4 is an expanded view of the heating/dispersion unit of the system of FIG. 1;
  • [0024]
    [0024]FIG. 5 is an expanded view of the reaction chamber of the system of FIG. 1; and
  • [0025]
    [0025]FIG. 6 is an expanded view of the separation unit of the system of FIG. 1.
  • [0026]
    The present invention provides a chemical or biochemical reactor that can be used for a variety of very small-scale techniques. In one embodiment, a microreactor of the invention comprises a matrix of a few millimeters to a few centimeters in size containing reaction channels with dimensions on the order of hundreds of microns. Reagents of interest are allowed to flow through these microchannels, mixed, and reacted together. The products can be recovered, separated, and treated within the system. While one microreactor may be able only to hold and react a few microliters of the substances of interest, the technology allows for easy scalability and tremendous parallelization. With enhanced oxygen and nutrient distribution, a microreactor of the invention demonstrates increased performance in terms of cell viability. The microreactor geometry resembles closely the natural environment of cells whereby diffusional oxygen and nutrient transfer take place through a high surface area, thin layer interface.
  • [0027]
    With regard to throughput, an array of many microreactors can be built in parallel to generate capacity on a level exceeding that allowed by current vessels and more uniform in product quality than can be obtained in a batch method. Additionally, an advantage is obtained by maintaining production capacity at the scale of reactions typically performed in the laboratory. In general, the coupled parameters for heat and mass transfer that are determined on the lab-scale for a process do not scale linearly with volume. With conventional reactors, as the magnitude of volume is increased 1,000-1,000,000 times for production, these parameters need to be re-evaluated, often involving a large capital-investment. The use of small production volumes, although scaled in parallel, reduces the cost of current scale-up schemes.
  • [0028]
    Furthermore, the process can be implemented on a simple platform, such as an etched article for example, a silicon wafer. With the effort of semiconductor manufacturing being towards the reduction in the dimensions of channels, an opportunity to utilize excess capacity within these production facilities (with unused equipment for the larger dimensions) is provided. Mass production of these units can be carried out at very low cost and an array of many reactors, for example thousands of microreactors typically can be built for a price lower than one traditional bioreactor.
  • [0029]
    Referring now to FIG. 1, a chemical or biochemical reactor in accordance with one embodiment of the invention is illustrated schematically. The reactor of FIG. 1 is, specifically, a microbioreactor for cell cultivation. It is to be understood that this is shown by way of example only, and the invention is not to be limited to this embodiment. For example, systems of the invention can be adapted for pharmaceutical production, hazardous chemical production, or chemical remediation of warfare reagents, etc.
  • [0030]
    Microreactor 10 includes four general units. A mixing unit 12, a heating/dispersion unit 14, a reaction unit 16, and a separation unit 18. That is, in the embodiment illustrated, processes of mixing, heating, reaction, purification are implemented in series. Although not shown, pressure, temperature, pH, and oxygen sensors can be included, for example embedded within the network to monitor and provide control for the system. Due to the series format, the opportunity for several reaction units in series for multi-step chemical syntheses, for several levels of increased purification, or for micro-analysis units is provided as well.
  • [0031]
    [0031]FIG. 1 shows microreactor 10 in expanded view. As illustrated, each of units 14 and 16 (heating/dispersion and reaction units, respectively) includes at least one adjacent temperature control element 20-26 including a channel 28 through which a temperature-control fluid can be made to flow. As illustrated, temperature control units 20 and 24 are positioned above and below unit 14 and units 22 and 26 are positioned above and below unit 16. Separation unit 18 includes upper and lower extraction solvent fluid units 30 and 32, respectively, separated from unit 18 by membranes 34 and 36, respectively.
  • [0032]
    Referring now to FIG. 2, reactor 10 is illustrated as assembled. The individual units of microreactor 10 will now be described in greater detail.
  • [0033]
    Referring now to FIG. 3, mixing unit 12 is illustrated. Mixing unit 12 is designed to provide a homogeneous mixture of starting materials or reactants to be provided to the reaction units, optionally via the heating/dispersion unit. In the specific example of the microbioreactor, mixing unit 12 is designed to provide a homogeneous broth with sufficient nutrients and oxygen, and at the required pH, for cells. Rather than combine the mixing process with simultaneous nourishment of the cells, the process is performed in a preliminary stage and then fed to the reaction stage where cells are immobilized. In this manner, the cells do not experience any shear stress due to mixing and a homogeneous mixture of feed requirements is guaranteed.
  • [0034]
    As is the case for other components of the reactor, mixing unit 12 can be manufactured using any convenient process. In preferred embodiments the unit is etched into a substrate such as silicon via known processes such as lithography. Other materials from which mixing unit 12, or other components of the systems of the. invention can be fabricated, include glass, fused silica, quartz, ceramics, or suitable plastics. Silicon is preferred. The mixing unit includes a plurality of inlets 40-50 which can receive any of a variety of reactants and/or fluid carriers. Although six inlets are illustrated, essentially any number of inlets from one to tens of hundreds of inlets can be provided. Typically, less than ten inlets are needed for a given reaction. Mixing unit 12 includes an outlet 52 and, between the plurality of inlets and the outlet, a mixing chamber 54 constructed and arranged to coalesce a plurality of reactant fluids provided through the inlets. It is a feature of the embodiment illustrated that the mixing chamber is free of active mixing elements. Instead, the mixing chamber is constructed to cause turbulence in the fluids provided through the inlets thereby mixing and delivering a mixture of the fluids through the outlet without active mixing. Specifically, the mixing unit includes a plurality of obstructions 56 in the flow path that causes mixture of fluid flowing through the flow path. These obstructions can be of essentially any geometrical arrangement. As illustrated, they define small pillars about which the fluid must turbulently flow as it passes from the inlets through the mixing chamber toward the outlet. As used herein “active mixing elements” is meant to define mixing elements such as blades, stirrers, or the like which are movable relative to the reaction chamber itself, that is, movable relative to the walls defining the reaction chamber.
  • [0035]
    The volume of the mixing chamber, that is, the volume of the interior of mixing unit 12 between the inlets and the outlet, can be very small in preferred embodiments. Specifically, the mixing chamber generally has a volume of less than one liter, preferably less than about 100 microliters, and in some embodiments less than about 10 microliters. The chamber can have a volume of less than about five microliters, or even less than about one microliter.
  • [0036]
    Specifically, in the microbioreactor illustrated, six separate feed streams empty into the mixing chamber under pressure. One feed stream provides gaseous oxygen (O2) as a cell requirement. One stream, respectively, provides carbon dioxide (CO2) and nitrogen (N2) for altering pH. The remaining three channels provide the broth solution including solvent and nutrients. One of these latter streams can also be utilized to provide any additional requirements for the system such as antifoaming agents. Antifoaming agents are sometimes necessary to prevent production of foam and bubbles that can damage cells within the broth. The feed of the various streams into the chamber provides enough turbulence for mixing of the different streams. Flow within microfluidic devices is characterized by a low Reynolds number indicating the formation of lamina. While the turbulence created by the injection streams should provide sufficient mixing before the development of laminar flow, pilon-like obstructions 56 are placed in the flow path of the stream leaving the primary mixing chamber in order to enhance mixing of the lamina. By splitting a main stream into substreams followed by reunification, turbulence is introduced in the flow path, and a mechanism other than simple diffusion is used to facilitate further mixing. The length of this mixing field can be lengthened or shortened depending on the system requirements.
  • [0037]
    Referring now to FIG. 4, heating/dispersion unit 14 is shown. Unit 14 can be formed as described above with respect to other units of the invention. Unit 14 includes an inlet 60 in fluid communication with a plurality of outlets 62 in embodiments where dispersion as described below is desirable. In operation, a stream of homogeneous fluid exiting the mixing unit (feed broth in the specific microbioreactor embodiment shown) enters a dispersion matrix defined by a plurality of obstructions dividing the stream into separate flow paths directed toward the separate outlets 62. The dispersion matrix is sandwiched between two temperature control elements 20 and 24 which, as illustrated, include fluid flow channels 28 etched in a silicon article. Control unit 24 is positioned underneath unit 14, thus etched channel 28 is sealed by the bottom of unit 14. Control unit 20 is positioned atop unit 14 such that the bottom of unit 20 seals and defines the top of diffusion unit 14. A cover (not shown) can be placed a top unit 20 to seal channel 28.
  • [0038]
    Rather than for mixing, as in the previous case (FIG. 3), the splitting of the streams is to disperse the medium for its entrance into the reactive chamber in the next unit operation. In traditional reactor systems, fluid flow about a packing material containing catalysts produces the desired reaction. However, if the fluid is not evenly dispersed entering the chamber, the fluid will flow through a low resistance path through the reactor and full, active surface area will not be utilized. Dispersion in this case is to optimize reactor efficiency in the next stage.
  • [0039]
    With regard to the heating function of this unit, the platform functions as a miniaturized, traditional heat exchanger. Etched silicon platforms both above and below the central platform serve to carry a heated fluid. Cells typically require their environment to have a temperature of ˜30 C. The fluids flowing in the etched coils both above and below the broth flow channel heating the broth through the thin silicon layer. The temperature of the fluid in the upper and lower heat exchangers can be modified to ensure proper temperature for the broth. Additionally, the platform can be extended for increased heating loads.
  • [0040]
    Although a combination heating/dispersion unit is shown, unit 14 can be either a dispersion unit or a heating unit. For example, dispersion can be provided as shown, without any temperature control. Alternatively, no dispersion need be provided (inlet 60 can communicate with a single outlet 62, which can be larger than the outlets as illustrated) and heating units can be provided. Cooling units can be provided as well, where cooling is desired. Units 20 and 24 can carry any temperature-control fluid, whether to heat or cool.
  • [0041]
    Referring now to FIG. 5, reaction chamber 16 is shown, including temperature control units 22 and 26, in expanded form. Units 22 and 26 can be the same as units 20 and 24 as shown in FIG. 4, with unit 22 defining the top of reaction chamber 16. Reaction unit 16 includes an inlet 70 fluidly communicating with an outlet 72 and a reaction chamber defined therebetween. The reaction chamber, in microreactor embodiments of the invention, has a volume of less than one milliliter, or other lower volumes as described above in connection with mixing unit 12. Inlet 70 is connectable to a source of a chemical or biological starting material, optionally supplied by mixing unit 12 and heating/dispersion unit 14, and outlet 70 is designed to release the product of a chemical or biological reaction occurring within the chamber involving the starting material. Unit 16 can be formed from materials as described above.
  • [0042]
    The reactor unit is the core of the process. While the unit is designed to be interchangeable for biological or pharmaceutical reactions, the specific application as shown is for cell cultivation. As in the case of the previous unit, temperature control units such as heat exchanger platforms will sandwich the central reaction chamber. The heat exchangers will maintain the temperature of the reaction unit at the same temperature as discussed for the cell broth.
  • [0043]
    A feature of the unit is heterogeneous reaction on a supported matrix. Cell feed enters the reaction chamber under the proper pH, O2 concentration, and temperature for cell cultivation. Cells, immobilized onto the silicon framework at locations 74 either by surface functionalization and subsequent reaction or entrapment within a host membrane, metabolize the nutrients provided by the feed stream and produce a product protein. The initial reaction platform can be a two-dimensional array of cells both on the top and bottom of the reaction chamber. This arrangement is to prevent a large pressure drop across the unit which would be detrimental to flow.
  • [0044]
    In this unit, oxygen and nutrients are diffused from the flowing stream to the immobilized cells. The cells, in turn metabolize the feed, and produce proteins which are swept away in the flowing stream. The flowing stream then enters the fourth chamber which removes the protein product from the solution.
  • [0045]
    Referring again to FIG. 1, it can be seen how dispersion unit 14 creates an evenly-divided flow of fluid (reactant fluid such as oxygen and nutrients in the case of cell cultivation) across each of locations 74 in reaction to chamber 16.
  • [0046]
    Referring now to FIG. 6, separation unit 18 is shown in greater detail, in expanded view. Separation unit 18 defines a central unit including an inlet 80 communicating with an outlet 82, and a fluid pathway 84 connecting the inlet with the outlet. Unit 18 can be fabricated as described above with respect to other components of the invention, and preferably is etched silicon. It may be desirable for fluid path 84 to completely span the thickness of unit 18 such that the pathway is exposed both above and below the unit. To maintain structural integrity, pathway 84 can be etched to some extent but not completely through unit 18 as illustrated, and a plurality of holes or channels can be formed through the bottom of the pathway exposing the bottom of the pathway to areas below the unit. Inlet 80 can be connectable to the outlet of reaction chamber 16, and outlet 82 to a container for recovery of carrier fluid.
  • [0047]
    In the embodiment illustrated, membranes 34 and 36 cover exposed portions of fluid pathway 84 facing upward or downward as illustrated. Membranes 30 and/or 36 can be any membranes suitable for separation, i.e. extraction of product through the membrane with passage of effluent, or carrier fluid, through outlet 82. Those of ordinary skill in the art will recognize a wide variety of suitable membranes including size-selective membranes, ionic membranes, and the like. Upper and lower extraction solvent fluid units 30 and 32, which can comprise materials as described above including etched silicon, each include a fluid pathway 86 connecting an inlet 88 with an outlet 90. Fluid pathway 86 preferably is positioned in register with fluid pathway 84 of unit 18 when the separation unit is assembled. In this way, two flowing streams of solvent through channels 86 of units 30 and 32 flow counter to the direction of flow of fluid in channel 84 of unit 18, the fluids separated only by membranes 34 and 36. This establishes a counter-current tangential flow filtration membrane system. By concentration gradients, products are selectively extracted from channel 84 into solvent streams flowing within channels 86 of unit 30 or 32. Product is recovered through the outlet 90 of units 30 or 32 and recovered in a container (not shown) having a volume that can be greater than 1 liter. Outlets 90 thereby define carrier fluid outlets, and a fluid pathway connects inlet 80 of unit 18 with the carrier fluid outlets 90 of units 30 and 32, breached only by membranes 34 and 36. Carrier fluid outlet 82 can be made connectable to a recovery container for recycling of reaction carrier fluids. In the example of a microbioreactor, residual oxygen and nutrients are recovered from outlet 82 and recycled back into the feed for the process.
  • [0048]
    The flowing streams of extraction solvent in channels 86 can be set at any desired temperature using temperature control units (not illustrated). In the case of a microbioreactor, these fluids can be set at approximately 4 C. The low temperature is needed to maintain the efficacy of the protein products and prevent denaturation. Additionally, several purification and clarification steps are often performed in industrial application. The necessity of further purification is remedied by the use of additional units in series.
  • [0049]
    Embedded within the production process can be control systems and detectors for the manipulation of temperature, pH, nutrients, and oxygen concentration. Where a microbioreactor is used, the viability of cells is dependent upon strict limits for the parameters mentioned above. Narrow set-point ranges, dependent on the cell system selected, can be maintained using thermocouples, pH detectors, O2 solubility detectors, and glucose detectors between each unit. These measurements will determine the heat exchanger requirements, O2, CO2, N2, and nutrient inputs.
  • [0050]
    Diaphragm and peristaltic pumps can be used to provide the necessary driving force for fluid flow in the units. Such pumps are also used to maintain flow in the heat exchanger units.
  • [0051]
    It is a feature of the invention that many of the microreactors as illustrated can be arranged in parallel. Specifically, at least ten reactors can be constructed to operate in parallel, or in other cases at least about 100, 500, 1,000, or even 10,000 reactors can be constructed to operate in parallel. These reactors can be assembled and disassembled as desired.
  • [0052]
    It is another feature of the invention that individual units 12, 14, 16, and 18 can be constructed and arranged to be connectable to and separable from each other. That is, any arrangement of individual components can be created for a desired reaction. For example, with reference to FIG. 1, heating/dispersion unit 14 may not be necessary. That is, outlet 52 of mixing unit 12 can be connectable to either inlet 60 of heating/dispersion unit 14, or inlet 70 of reaction unit 16 where a heating/dispersion unit is not used. Moreover, assembly and disassembly of reactors to create a system including many, many reactors operating in parallel, as described above, or in series is possible because of the connectability and separability of the components from each other to form systems containing specific desired components, and any number of those or other systems operating together. Equipment for connection and separation of individual components of a reactor can be selected among those known in the art, as can systems for connection of a variety of reactors in parallel or in series. Systems should be selected such that the individual components can be connectable to and separable from each other readily by laboratory or production-facility technicians without irreversible destruction of components such as welding, sawing, or the like. Examples of known systems for making readily reversible connections between components of reactors or between reactors to form parallel reactors or series reactors include male/female interconnections, clips, cartridge housings where components comprise inserts within the housings, screws, or the like.
  • [0053]
    Those skilled in the art would readily appreciate that all parameters listed herein are meant to be exemplary and that actual parameters will depend upon the specific application for which the methods and apparatus of the present invention are used. It is, therefore, to be understood that the foregoing embodiments are presented by way of example only and that, within the scope of the appended claims and equivalents thereto, the invention may be practiced otherwise than as specifically described. In the claims the words “including”, “carrying”, “having”, and the like mean, as “comprising”, including but not limited to.
Patent Citations
Cited PatentFiling datePublication dateApplicantTitle
US4038151 *Jul 29, 1976Jul 26, 1977Mcdonnell Douglas CorporationCard for use in an automated microbial detection system
US4318994 *Feb 26, 1981Mar 9, 1982Mcdonnell Douglas CorporationEnterobacteriaceae species biochemical test card
US4720462 *Nov 5, 1985Jan 19, 1988Robert RosensonCulture system for the culture of solid tissue masses and method of using the same
US4756884 *Jul 1, 1986Jul 12, 1988Biotrack, Inc.Capillary flow device
US4839292 *Sep 11, 1987Jun 13, 1989Cremonese Joseph GCell culture flask utilizing a membrane barrier
US5219762 *Dec 20, 1989Jun 15, 1993Mochida Pharmaceutical Co., Ltd.Method and device for measuring a target substance in a liquid sample
US5278048 *May 29, 1991Jan 11, 1994Molecular Devices CorporationMethods for detecting the effect of cell affecting agents on living cells
US5387329 *Apr 9, 1993Feb 7, 1995Ciba Corning Diagnostics Corp.Extended use planar sensors
US5424209 *Mar 19, 1993Jun 13, 1995Kearney; George P.Automated cell culture and testing system
US5436129 *Oct 12, 1993Jul 25, 1995Gene Tec Corp.Process for specimen handling for analysis of nucleic acids
US5496697 *Sep 8, 1993Mar 5, 1996Molecular Devices CorporationMethods and apparatus for detecting the effect of cell affecting agents on living cells
US5534328 *Dec 2, 1993Jul 9, 1996E. I. Du Pont De Nemours And CompanyIntegrated chemical processing apparatus and processes for the preparation thereof
US5595712 *Jul 25, 1994Jan 21, 1997E. I. Du Pont De Nemours And CompanyChemical mixing and reaction apparatus
US5602028 *Jun 30, 1995Feb 11, 1997The University Of British ColumbiaSystem for growing multi-layered cell cultures
US5612188 *Feb 10, 1994Mar 18, 1997Cornell Research Foundation, Inc.Automated, multicompartmental cell culture system
US5632957 *Sep 9, 1994May 27, 1997NanogenMolecular biological diagnostic systems including electrodes
US5639423 *Aug 31, 1992Jun 17, 1997The Regents Of The University Of CalforniaMicrofabricated reactor
US5646039 *Jun 6, 1995Jul 8, 1997The Regents Of The University Of CaliforniaMicrofabricated reactor
US5705018 *Dec 13, 1995Jan 6, 1998Hartley; Frank T.Micromachined peristaltic pump
US5856174 *Jan 19, 1996Jan 5, 1999Affymetrix, Inc.Integrated nucleic acid diagnostic device
US5858770 *Sep 30, 1997Jan 12, 1999Brandeis UniversityCell culture plate with oxygen and carbon dioxide-permeable waterproof sealing membrane
US5916812 *May 13, 1997Jun 29, 1999Biomerieux, Inc.Test sample card with polymethylpentene tape
US5928880 *Jun 11, 1997Jul 27, 1999Trustees Of The University Of PennsylvaniaMesoscale sample preparation device and systems for determination and processing of analytes
US6012902 *Sep 25, 1997Jan 11, 2000Caliper Technologies Corp.Micropump
US6042710 *May 11, 1999Mar 28, 2000Caliper Technologies Corp.Methods and compositions for performing molecular separations
US6043080 *Dec 11, 1998Mar 28, 2000Affymetrix, Inc.Integrated nucleic acid diagnostic device
US6046056 *Dec 6, 1996Apr 4, 2000Caliper Technologies CorporationHigh throughput screening assay systems in microscale fluidic devices
US6167910 *Jan 14, 1999Jan 2, 2001Caliper Technologies Corp.Multi-layer microfluidic devices
US6171067 *Oct 20, 1999Jan 9, 2001Caliper Technologies Corp.Micropump
US6171850 *Mar 8, 1999Jan 9, 2001Caliper Technologies Corp.Integrated devices and systems for performing temperature controlled reactions and analyses
US6186660 *Jul 26, 1999Feb 13, 2001Caliper Technologies Corp.Microfluidic systems incorporating varied channel dimensions
US6193647 *Apr 8, 1999Feb 27, 2001The Board Of Trustees Of The University Of IllinoisMicrofluidic embryo and/or oocyte handling device and method
US6235175 *Oct 2, 1998May 22, 2001Caliper Technologies Corp.Microfluidic devices incorporating improved channel geometries
US6238538 *Apr 6, 1999May 29, 2001Caliper Technologies, Corp.Controlled fluid transport in microfabricated polymeric substrates
US6245295 *Feb 23, 1999Jun 12, 2001Bio Merieux, Inc.Sample testing apparatus with high oxygen permeable tape providing barrier for closed reaction chamber
US6251343 *Feb 24, 1998Jun 26, 2001Caliper Technologies Corp.Microfluidic devices and systems incorporating cover layers
US6264892 *Jan 11, 2000Jul 24, 2001Agilent Technologies, Inc.Miniaturized planar columns for use in a liquid phase separation apparatus
US6267858 *Jun 24, 1997Jul 31, 2001Caliper Technologies Corp.High throughput screening assay systems in microscale fluidic devices
US6338790 *Apr 21, 1999Jan 15, 2002Therasense, Inc.Small volume in vitro analyte sensor with diffusible or non-leachable redox mediator
US6346413 *Nov 17, 1999Feb 12, 2002Affymetrix, Inc.Polymer arrays
US6368871 *Aug 13, 1997Apr 9, 2002CepheidNon-planar microstructures for manipulation of fluid samples
US6377721 *Mar 2, 1999Apr 23, 2002Trustees Of Tufts CollegeBiosensor array comprising cell populations confined to microcavities
US6410309 *Nov 28, 2000Jun 25, 2002Biocrystal LtdCell culture apparatus and methods of use
US6509085 *Apr 10, 2000Jan 21, 2003Caliper Technologies Corp.Fabrication of microfluidic circuits by printing techniques
US6517234 *Nov 2, 2000Feb 11, 2003Caliper Technologies Corp.Microfluidic systems incorporating varied channel dimensions
US6551841 *Jan 27, 1999Apr 22, 2003The Trustees Of The University Of PennsylvaniaDevice and method for the detection of an analyte utilizing mesoscale flow systems
US6569674 *Jan 26, 2000May 27, 2003Amersham Biosciences AbMethod and apparatus for performing biological reactions on a substrate surface
US6582576 *Oct 7, 1999Jun 24, 2003Caliper Technologies Corp.Controller/detector interfaces for microfluidic systems
US6592821 *May 10, 2001Jul 15, 2003Caliper Technologies Corp.Focusing of microparticles in microfluidic systems
US6597438 *Aug 2, 2000Jul 22, 2003Honeywell International Inc.Portable flow cytometry
US6689594 *Jun 4, 1999Feb 10, 2004Haenni ClaudeDevice for organic cell culture and for studying their electrophysiological activity and membrane used in said device
US6716588 *Dec 8, 2000Apr 6, 2004Cellomics, Inc.System for cell-based screening
US6716620 *Mar 26, 2001Apr 6, 2004Purdue Research FoundationBiosensor and related method
US6716629 *Oct 10, 2001Apr 6, 2004Biotrove, Inc.Apparatus for assay, synthesis and storage, and methods of manufacture, use, and manipulation thereof
US6742661 *Aug 17, 2001Jun 1, 2004Micronics, Inc.Well-plate microfluidics
US6756019 *Apr 6, 2000Jun 29, 2004Caliper Technologies Corp.Microfluidic devices and systems incorporating cover layers
US6837927 *Jan 29, 2002Jan 4, 2005Syrrx, Inc.Microvolume device employing fluid movement by centrifugal force
US6857449 *Sep 30, 2003Feb 22, 2005Caliper Life Sciences, Inc.Multi-layer microfluidic devices
US20020029814 *Apr 6, 2001Mar 14, 2002Marc UngerMicrofabricated elastomeric valve and pump systems
US20020055166 *Oct 2, 2001May 9, 2002Cannon Thomas F.Automated bioculture and bioculture experiments system
US20020068358 *Apr 5, 2001Jun 6, 2002Campbell Michael J.In vitro embryo culture device
US20020072116 *Oct 12, 2001Jun 13, 2002Bhatia Sangeeta N.Nanoporous silicon bioreactor
US20020086439 *Oct 17, 2001Jul 4, 2002Caliper Technologies Corp.Integrated devices and systems for performing temperature controlled reactions and analyses
US20020092767 *Nov 28, 2001Jul 18, 2002Aclara Biosciences, Inc.Multiple array microfluidic device units
US20020097633 *Jan 11, 2002Jul 25, 2002Nanostream,Inc.Multi-stream microfluidic mixers
US20030008308 *Apr 5, 2002Jan 9, 2003California Institute Of TechnologyNucleic acid amplification utilizing microfluidic devices
US20030008388 *Jun 25, 2002Jan 9, 2003Biocrystal, Ltd.Cell culture apparatus and methods of use
US20030010104 *May 16, 2002Jan 16, 2003Byeong-Wook JeonLearning method for an automatic transmission of a vehicle and a system thereof
US20030013203 *Jul 29, 2002Jan 16, 2003ZyomyxMicrofluidic devices and methods
US20030015429 *Sep 3, 2002Jan 23, 2003Caliper Technologies Corp.Methods, devices and systems for characterizing proteins
US20030022153 *Mar 15, 2002Jan 30, 2003Gregory KirkMethod of monitoring haptotaxis
US20030022197 *Mar 15, 2002Jan 30, 2003Greg KirkDevice for monitoring haptotaxis
US20030022203 *Apr 23, 2002Jan 30, 2003Rajan KumarCellular Arrays
US20030022269 *Mar 15, 2002Jan 30, 2003Gregory KirkMethod of monitoring cell motility and chemotaxis
US20030022362 *Mar 15, 2002Jan 30, 2003Gregory KirkCell motility and chemotaxis test device and methods of using same
US20030026740 *Aug 5, 2002Feb 6, 2003Staats Sau Lan TangMicrofluidic devices
US20030049862 *May 24, 2002Mar 13, 2003Lin HeMicrocolumn-based, high-throughput microfluidic device
US20030077817 *Apr 10, 2002Apr 24, 2003Zarur Andrey J.Microfermentor device and cell based screening method
US20030082632 *Jul 23, 2002May 1, 2003Cytoprint, Inc.Assay method and apparatus
US20030082795 *Apr 25, 2002May 1, 2003Michael ShulerDevices and methods for pharmacokinetic-based cell culture system
US20030104512 *Nov 30, 2001Jun 5, 2003Freeman Alex R.Biosensors for single cell and multi cell analysis
US20030129665 *Aug 29, 2002Jul 10, 2003Selvan Gowri PyapaliMethods for qualitative and quantitative analysis of cells and related optical bio-disc systems
US20030134431 *Oct 24, 2002Jul 17, 2003Caliper Technologies Corp.High throughput screening assay systems in microscale fluidic devices
US20030142291 *Nov 26, 2002Jul 31, 2003Aravind PadmanabhanPortable scattering and fluorescence cytometer
US20040002131 *Mar 12, 2003Jan 1, 2004Enoch KimCell motility and chemotaxis test device and methods of using same
US20040029213 *Jun 7, 2001Feb 12, 2004Callahan Daniel E.Visual-servoing optical microscopy
US20040029266 *Aug 9, 2002Feb 12, 2004Emilio Barbera-GuillemCell and tissue culture device
US20040053403 *Jun 24, 2003Mar 18, 2004ZyomyxMicrofluidic devices and methods
US20040058407 *Jun 5, 2003Mar 25, 2004Miller Scott E.Reactor systems having a light-interacting component
US20040058408 *Aug 28, 2003Mar 25, 2004Gyros AbMicrofabricated apparatus for cell based assays
US20040058437 *Jun 5, 2003Mar 25, 2004Rodgers Seth T.Materials and reactor systems having humidity and gas control
US20040067577 *Oct 8, 2002Apr 8, 2004Wilson Wilbur W.Micro-fluidic device for monitoring biomolecular interactions
US20040072278 *Apr 1, 2003Apr 15, 2004Fluidigm CorporationMicrofluidic particle-analysis systems
US20040077075 *May 1, 2003Apr 22, 2004Massachusetts Institute Of TechnologyMicrofermentors for rapid screening and analysis of biochemical processes
US20050014129 *Aug 6, 2002Jan 20, 2005David CliffelDevice and methods for detecting the response of a plurality of cells to at least one analyte of interest
US20050037471 *Apr 30, 2004Feb 17, 2005California Institute Of TechnologyMicrofluidic rotary flow reactor matrix
US20050047967 *Sep 3, 2003Mar 3, 2005Industrial Technology Research InstituteMicrofluidic component providing multi-directional fluid movement
US20050089993 *Apr 1, 2004Apr 28, 2005Paolo BoccazziApparatus and methods for simultaneous operation of miniaturized reactors
Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US7276351Oct 17, 2003Oct 2, 2007Seahorse BioscienceMethod and device for measuring multiple physiological properties of cells
US7638321Jun 1, 2007Dec 29, 2009Seahorse Bioscience, Inc.Method and device for measuring multiple physiological properties of cells
US7795359Mar 1, 2006Sep 14, 2010Novartis AgContinuous process for production of polymeric materials
US7851201Nov 9, 2009Dec 14, 2010Seahorse Bioscience, Inc.Method and device for measuring multiple physiological properties of cells
US8119079 *Mar 24, 2008Feb 21, 2012Samsung Electronics Co., Ltd.Microfluidic apparatus having fluid container
US8202702Oct 14, 2009Jun 19, 2012Seahorse BioscienceMethod and device for measuring extracellular acidification and oxygen consumption rate with higher precision
US8658349Jul 13, 2006Feb 25, 2014Seahorse BioscienceCell analysis apparatus and method
US8697431May 19, 2010Apr 15, 2014Seahorse Bioscience, Inc.Method and device for measuring multiple physiological properties of cells
US9138745 *Feb 8, 2013Sep 22, 2015Rohm Co., Ltd.Microchip
US9170253Mar 4, 2014Oct 27, 2015Seahorse BioscienceMethod and device for measuring multiple physiological properties of cells
US9170255Jan 8, 2014Oct 27, 2015Seahorse BioscienceCell analysis apparatus and method
US9494577Nov 13, 2013Nov 15, 2016Seahorse BiosciencesApparatus and methods for three-dimensional tissue measurements based on controlled media flow
US20030077817 *Apr 10, 2002Apr 24, 2003Zarur Andrey J.Microfermentor device and cell based screening method
US20040197905 *Jan 16, 2004Oct 7, 2004Thermogenic ImaginingMethods and devices for monitoring cellular metabolism in microfluidic cell-retaining chambers
US20050054028 *Oct 17, 2003Mar 10, 2005Thermogenic ImagingMethod and device for measuring multiple physiological properties of cells
US20060019333 *Jun 7, 2005Jan 26, 2006Rodgers Seth TControl of reactor environmental conditions
US20060241242 *Mar 1, 2006Oct 26, 2006Devlin Brian GContinuous process for production of polymeric materials
US20070087401 *Oct 10, 2006Apr 19, 2007Andy NeilsonAnalysis of metabolic activity in cells using extracellular flux rate measurements
US20070217964 *Feb 15, 2007Sep 20, 2007Johnson Timothy JMicroreactor with auxiliary fluid motion control
US20070238165 *Jun 1, 2007Oct 11, 2007Seahorse BioscienceMethod and device for measuring multiple physiological properties of cells
US20080014571 *Jul 13, 2006Jan 17, 2008Seahorse BioscienceCell analysis apparatus and method
US20080081842 *Sep 30, 2007Apr 3, 2008Fujifilm CorporationEmulsion and method of manufacturing emulsion
US20080305006 *Mar 24, 2008Dec 11, 2008Samsung Electronics Co., Ltd.Microfluidic apparatus having fluid container
US20100105578 *Nov 9, 2009Apr 29, 2010Seahorse BioscienceMethod and device for measuring multiple physiological properties of cells
US20100124761 *Oct 14, 2009May 20, 2010Neilson Andy CMethod and device for measuring extracellular acidification and oxygen consumption rate with higher precision
US20100185004 *Jul 9, 2007Jul 22, 2010Evonik Degussa GmbhSystem, reactor and process for the continuous industrial production of polyetheralkylalkoxysilanes
US20100227385 *May 19, 2010Sep 9, 2010Seahorse BioscienceMethod and device for measuring multiple physiological properties of cells
US20110041986 *Nov 5, 2010Feb 24, 2011Dai Nippon Printing Co., Ltd.Micro-reactor and method of manufacturing the same
US20110220332 *Mar 12, 2010Sep 15, 2011Analogic CorporationMicro channel device temperature control
US20120142118 *May 27, 2010Jun 7, 2012Cornell UniversityMicrofabrication of high temperature microreactors
US20130209329 *Feb 8, 2013Aug 15, 2013Rohm Co., Ltd.Microchip
EP1905505A2 *Sep 26, 2007Apr 2, 2008FUJIFILM CorporationMethod of manufacturing an emulsion, and emulsion so produced
EP1905505A3 *Sep 26, 2007May 28, 2008FUJIFILM CorporationMethod of manufacturing an emulsion, and emulsion so produced
WO2004065618A2 *Jan 14, 2004Aug 5, 2004Thermogenic ImagingMethods and devices for monitoring cellular metabolism in microfluidic cell-retaining chambers
WO2004065618A3 *Jan 14, 2004Aug 24, 2006Thermogenic ImagingMethods and devices for monitoring cellular metabolism in microfluidic cell-retaining chambers
WO2007098027A2 *Feb 15, 2007Aug 30, 2007Bioprocessors Corp.Microreactor with auxiliary fluid motion control
WO2007098027A3 *Feb 15, 2007Oct 25, 2007Bioprocessors CorpMicroreactor with auxiliary fluid motion control
U.S. Classification435/288.5, 435/289.1
International ClassificationC12M1/00, C12P21/00, G01N37/00, B01J19/24, B81B1/00, C12P1/00, B81B7/04, G01N33/53, B01F13/00, B01F5/02, B01F5/06, B01J19/00, C12M3/00
Cooperative ClassificationB01J2219/00957, B01J2219/00835, B01J2219/00873, B01F5/0647, B01F13/0094, B01F5/0256, B01J2219/00783, B01F2005/0621, B01J2219/00961, B01J2219/00966, B01J2219/00828, B01J2219/00871, B01J2219/00907, B01J2219/00963, B01F5/061, B01J19/0093, B01F15/00935, C12M23/16, B01J2219/00862, B01F5/0646, B01F13/0064, B01J2219/00889
European ClassificationB01F13/00M6J, B01F15/00T2, B01F5/06B3F2, C12M23/16, B01F5/06B3F, B01F5/06B3B, B01F13/00M2B, B01J19/00R, B01F5/02C
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May 20, 2005ASAssignment
Owner name: STARLAB N.V./S.A., BELGIUM
Effective date: 20001219
Owner name: STARLAB N.V./S.A., BELGIUM
Effective date: 20031030
Effective date: 20001218