US20010032814A1 - Shallow bed fluid treatment apparatus - Google Patents

Shallow bed fluid treatment apparatus Download PDF

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Publication number
US20010032814A1
US20010032814A1 US09/769,881 US76988101A US2001032814A1 US 20010032814 A1 US20010032814 A1 US 20010032814A1 US 76988101 A US76988101 A US 76988101A US 2001032814 A1 US2001032814 A1 US 2001032814A1
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Prior art keywords
fluid
bed
distributor
processing
collector
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US09/769,881
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Michael Kearney
Kenneth Peterson
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Amalgamated Research LLC
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Amalgamated Research LLC
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Priority to US09/769,881 priority Critical patent/US20010032814A1/en
Assigned to AMALGAMATED RESEARCH, INC. reassignment AMALGAMATED RESEARCH, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: KEARNEY, MICHAEL M., PETERSON, KENNETH R., VELASQUEZ, LAWRENCE
Publication of US20010032814A1 publication Critical patent/US20010032814A1/en
Assigned to AMALGAMATED RESEARCH, INC. reassignment AMALGAMATED RESEARCH, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: KEARNEY, MICHAEL M., PETERSEN, KENNETH R., VELASQUEZ, LAWRENCE
Priority to US10/867,968 priority patent/US7390408B2/en
Abandoned legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
    • B01D15/08—Selective adsorption, e.g. chromatography
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
    • B01D15/08—Selective adsorption, e.g. chromatography
    • B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
    • B01D15/14—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to the introduction of the feed to the apparatus
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/40—Static mixers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/71—Feed mechanisms
    • B01F35/717—Feed mechanisms characterised by the means for feeding the components to the mixer
    • B01F35/7182—Feed mechanisms characterised by the means for feeding the components to the mixer with means for feeding the material with a fractal or tree-type distribution in a surface
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J47/00—Ion-exchange processes in general; Apparatus therefor
    • B01J47/02—Column or bed processes
    • B01J47/022—Column or bed processes characterised by the construction of the column or container
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
    • B01J8/025—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical shaped bed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0278—Feeding reactive fluids
    • G—PHYSICS
    • G01—MEASURING; TESTING
    • G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
    • G01N30/00—Investigating or analysing materials by separation into components using adsorption, absorption or similar phenomena or using ion-exchange, e.g. chromatography or field flow fractionation
    • G01N30/02—Column chromatography
    • G01N30/60—Construction of the column
    • G01N30/6004—Construction of the column end pieces
    • G01N30/6017—Fluid distributors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/40—Static mixers
    • B01F25/41—Mixers of the fractal type
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/18—Details relating to the spatial orientation of the reactor
    • B01J2219/185—Details relating to the spatial orientation of the reactor vertical
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/19—Details relating to the geometry of the reactor
    • B01J2219/194—Details relating to the geometry of the reactor round
    • B01J2219/1941—Details relating to the geometry of the reactor round circular or disk-shaped
    • B01J2219/1943—Details relating to the geometry of the reactor round circular or disk-shaped cylindrical
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B33—ADDITIVE MANUFACTURING TECHNOLOGY
    • B33Y—ADDITIVE MANUFACTURING, i.e. MANUFACTURING OF THREE-DIMENSIONAL [3-D] OBJECTS BY ADDITIVE DEPOSITION, ADDITIVE AGGLOMERATION OR ADDITIVE LAYERING, e.g. BY 3-D PRINTING, STEREOLITHOGRAPHY OR SELECTIVE LASER SINTERING
    • B33Y80/00—Products made by additive manufacturing
    • G—PHYSICS
    • G01—MEASURING; TESTING
    • G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
    • G01N30/00—Investigating or analysing materials by separation into components using adsorption, absorption or similar phenomena or using ion-exchange, e.g. chromatography or field flow fractionation
    • G01N30/02—Column chromatography
    • G—PHYSICS
    • G01—MEASURING; TESTING
    • G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
    • G01N30/00—Investigating or analysing materials by separation into components using adsorption, absorption or similar phenomena or using ion-exchange, e.g. chromatography or field flow fractionation
    • G01N30/02—Column chromatography
    • G01N30/60—Construction of the column
    • G01N30/6052—Construction of the column body
    • G01N30/6069—Construction of the column body with compartments or bed substructure

Definitions

  • Fluid processes characteristically exhibit severe limits on operation due to bed pressure drop, kinetics and flow uniformity. These limits are placed on, for example, productivity, process efficiency, energy use, system size, environmental compatibility, and capital/operating costs.
  • the flow rate through a bed may be constrained because as flow rate increases, bed pressure drop increases. Pressure drop may reach a point where the pressure rating of a column containing the bed may be exceeded, the bed may begin to unacceptably compress, bed particles may be destroyed and excessive energy may be required for operation. Clearly, this effect places limits on productivity (limits on flow rate) and cell design and cost (higher pressure requires additional structural strength).
  • a representative device is disclosed in U.S. Pat. No. 4,673,507 to Brown.
  • the '507 patent discloses a fluid treatment apparatus which can be used for shallow bed operation.
  • this device lacks significantly distributed fluid feed and collection systems and is dependent upon maintaining the bed in an over packed condition.
  • a substantially uniform fluid flow distribution across the bed is achieved by employing resins of fine (substantially uniform) particle size which are maintained in an over packed condition.
  • the term ‘over packed’ is used to mean that the particles are confined within the resin bed so that they are subjected to compression at all times. This device inherently restricts process fluid flow across the bed.
  • U.S. Pat. No. 5,626,750 to Chinn discloses an apparatus for treating fluid.
  • first and second “particle free cavities” are provided above and below the retained particle bed. Even flow of fluid through the bed is provided simply by the pressure drop across the bed. The pressure drop across the bed is a function of the pressures in the first and second cavities. No provision is made to substantially control fluid flow characteristics (eddies, or turbulent zones) in process fluid streams near the bed surface.
  • the present invention provides an apparatus for a fluid processing system which involves passing a fluid through a processing bed configured to have a diameter substantially greater than it's height (the distance between its inlet end and its outlet end).
  • the invention is operable in systems in which the ratio of diameter (D) to height (h) of the processing bed is as high as 20:1 or more.
  • the invention is advantageously applied to beds with D:h ratios approaching 2:1, but D:h ratios in excess of about 3:1 are presently preferred.
  • processing bed refers to any confined mass of conventional or special purpose processing material (medium) contained by a cell or column through which fluids are passed. Typical such processing materials include inorganic or organic packing materials, chromatographic media, ion exchange media, absorption or adsorption media, enzymes and catalytic reactants.
  • a fluid distributor is typically arranged to introduce process fluid at the inlet end of the bed with a density of at least 200 distribution exits per square foot.
  • a fluid collector is typically arranged to collect once processed fluid at the outlet end of the resin bed. It is generally preferred for the collector to be arranged to collect fluid through collection inlets with a density of at least 200 per square foot. It is within contemplation to provide inlets and/or exits with a density of 200 per square inch or more. It is currently preferred to construct the distributor and the collector from recursively arranged fractal elements. Systems according to the principles of the present invention may be constructed to produce processing flow conditions with a pressure drop across the media bed of less than 5 psi.
  • a system according to the present invention may further include a second processing bed with an inlet side, an outlet side, and a diameter at least twice the distance between the inlet side and the outlet side.
  • a second fluid distributor may be arranged to introduce the once processed fluid to the inlet side of the second bed.
  • the second distributor also desirably has a density of at least 200 distribution exits per square foot to promote one-dimensional flow with minimized mixing and turbulence in the process fluid.
  • a second fluid collector is then generally arranged to collect twice processed fluid at the outlet side of the second resin bed.
  • the first and second fluid distributors may be formed from fractal structure. It is also preferred that the first and second fluid collectors are formed from fractal structure, and are similar to the distributors.
  • One desirable recursive fractal element may be characterized as having an “H” shape. Other fractal elements, including those with 3-dimensional shapes, are also within contemplation for use in either distributor or collector structures.
  • FIG. 1 is a plan view in cross-section of a typical embodiment of this invention
  • FIG. 2 is a close-up of an edge portion indicated by arrows 2 - 2 in FIG. 1;
  • FIG. 3 is a plan view in cross-section of an alternate embodiment of this invention having a void space left between the bed and the top distributor;
  • FIG. 4 is a plan view of an embodiment having supports for the end distributors
  • FIG. 5 is a top view of a typical top end plate
  • FIG. 6 is a top view of a representative fractal distributor embodiment
  • FIG. 7 is a top view of an alternative embodiment, similar to the fractal distributor of FIG. 6, but with an additional fractal iteration partially illustrated at the outside periphery.
  • FIG. 1 illustrates a typical fluid treatment apparatus according to this invention, generally indicated at 102 .
  • the apparatus typically includes a top plate 106 , a bottom plate 110 , and a side wall 112 .
  • side wall 112 forms a ring-like structure to enclose a volume between top and bottom plates 106 and 110 .
  • the apparatus will be described with reference to a substantially circular side wall 112 , although such a structural limitation is not required for practice of this invention.
  • One or more side walls 112 may be constructed to form virtually any shape in cross-section through the apparatus.
  • top and bottom plates 106 and 110 it is currently preferred to assemble top and bottom plates 106 and 110 to side wall 112 in fluid tight engagement with top and bottom gaskets 114 and 116 respectively.
  • Joint structure which may be disassembled is generally preferred, such as the bolted joint interface indicated generally at 120 , in the assembly of an apparatus 102 .
  • top plate 106 generally carries one or more fluid ports 124 for passing process fluids there through.
  • Fluid port 124 is desirably constructed in fluid communication with a distribution network of orifices arranged in a fractal distributor 128 .
  • a distributor 128 preferably functions to distribute the process fluid in a configuration approaching a homogeneous arrangement of inlet or exit points in space. The main purpose of such a distributor is to produce process fluid flow directed in substantially only one direction. It is currently preferred to provide distributor 128 as a fractal.
  • a bed 132 formed of a suitable working media, is typically disposed between fractal distributors 128 and 136 .
  • distributor 136 In operation under top-down flow, distributor 136 functions as a collector.
  • a distributor 136 is typically similar in structure to the distributor 128 , but in any case generally provides a homogeneous arrangement of inlet or exit points in space.
  • Fluid port 138 in fluid communication with distributor 136 , functions to pass process fluids through bottom plate 110 . It may now be realized that process fluids introduced into apparatus 102 through port 124 may pass through bed 132 and be collected for exit through port 138 . Process fluid may be distributed and collected in a substantially homogeneous fashion by fractal distributors 128 and 136 on —opposite sides of the bed 132 .
  • the distributors 128 and 136 minimize turbulence and mixing in the process fluid in zones near the top and bottom surfaces of bed 132 .
  • Process fluid flow may alternatively be oppositely directed, with port 138 functioning as an inlet, and port 128 as an outlet port.
  • port 138 functioning as an inlet
  • port 128 functioning as an outlet port.
  • the apparatus will generally be described hereinafter with a top-down flow condition.
  • top distributor 128 functions as a distributor
  • bottom distributor 136 functions as a collector.
  • FIG. 2 illustrates a close-up view of structure typically included in preferred embodiments of the invention.
  • the illustration of FIG. 2 depicts typical mirror image construction on inlet and outlet sides of the device.
  • Three zones are indicated through the height of the apparatus, representing a fractal distributor zone 142 , a bed zone 144 , and a second fractal distributor zone 146 .
  • Fractal distributor zone 142 houses fractal distributor 128
  • fractal distributor zone 146 houses fractal distributor 136 .
  • the distributor zones do not have to fill the entire space between the bed 132 and the top or bottom plates 106 and 110 respectively.
  • a space may be maintained, for example, above a bed 132 for purpose of fluidizing the bed 132 .
  • the fractal distributor zones typically function to minimize mixing and turbulence near the bed surfaces.
  • a distributor 128 or 136 desirably provides a population of fluid exits at a fluid/distributor interface to approximate a distributed fluid flow having only a component of velocity directed toward, or away from, a surface of the bed 132 .
  • Bed zone 144 houses bed 132 having top and bottom surfaces 148 and 150 respectively.
  • Bed zone 144 may be defined by top and bottom surfaces formed by a screen, mesh, membrane, or other retaining elements (not illustrated).
  • FIG. 3 illustrates an alternative embodiment 154 of this invention with a void space 156 left between the bed 132 and the top distributor 128 .
  • the invention can operate efficiently in this configuration.
  • This alternative embodiment 154 allows for internal fluidization which is necessary for common steps such as bed backwash or continuous fluidized bed operation.
  • Void space 156 allows material of bed 132 sufficient space in which to move in a vertical direction for purpose of backwashing or to fluidize the bed 132 .
  • FIG. 4 illustrates internal supports 160 which can be used if the diameter of the shallow cell becomes too large to properly support the end distributors.
  • the supports 160 preferably intersect the fractal distributors 128 and 136 in blank areas to avoid any interference with process fluid flow.
  • Rods or flat plate are examples of support structure which can be used in a support element 160 .
  • FIG. 5 illustrates a top end plate 106 with a fluid port 124 located approximately on a central axis.
  • One or more such ports 124 may be located at other, non axial locations. However, it is currently preferred to have only one such port 124 centrally located through end plate 106 .
  • the location of the port 124 may be determined by manufacturing concerns, and may thus be off centered. It is generally desired to provide port 124 at a location convenient for connection with distributor 128 .
  • a plurality of bolt holes 164 may be provided spaced around the perimeter of illustrated plate 106 to form joint structure 120 .
  • a bottom end plate 110 is typically structured similar to, or symmetric to, top plate 106 .
  • FIG. 6 illustrates a typical fractal distributor embodiment 128 appropriate for this apparatus.
  • the illustrated embodiment is only exemplary of a distributor 128 , and represents only one desirable arrangement of distribution structure.
  • a virtually infinite number of variations in structural configuration of a distributor 128 are workable.
  • conduits forming the distributor system 128 are placed on separate planes and do not intersect. Arcuate sectors 164 and 168 are illustrated in progressive stages of assembly. Fluid introduced to port 124 is divided to flow through successively divided conduit branches. As illustrated, fluid flowing from port 124 is divided into six conduits 172 . Each of conduits 172 may subsequently be divided into three or six conduits 174 (can be mirror imaged in planes above and below conduits 172 ). Conduits 174 are then divided for fluid flow into multiple conduits 176 . The recursive division process may be continued as desired to provide a sufficient density of fluid exits or entrances.
  • each successive division of conduits at least doubles the number of exits into the cell, and increasingly spreads the exits out into a distribution more uniform throughout the volume occupied by a distributor 128 .
  • Exits are not necessarily oriented to have an opening directed in the direction of overall flow from a distributor toward a bed. Simply spreading out the exits uniformly in a volume occupied by the distributor 128 promotes one-dimensional flow toward a bed 132 , and minimizes turbulence in the process fluid.
  • fractal refers to a device constructed as a distributor or collector ( 128 or 136 ) having outlets or inlets connected through conduits constructed and arranged substantially in accordance with the principles of fractal geometry. Fractal structures are mathematical constructs which exhibit scale invariance. In such structures a self-similar geometry recurs at many scales. Typical distributors or collectors 128 or 136 are desirably configured of conduit arranged in fractal patterns using any well known fabrication technique, such as matrices of pipe, molded or machined tiles, or stamped plate. The outlet or inlet orifice density can be increased by recursively duplicating a basic pattern (fractal) on smaller and smaller scale.
  • a most simple fractal is a simple “T” intersection formed by intersecting a first conduit at a right angle with a second, generally smaller diameter, conduit. This simplest case doubles the number of inlets or outlets in a distribution system with each successive generation of fractal structure. Outlets of each generation of fractal structures are typically connected to inlets of the subsequent fractal generation. The outlets of the final generation of fractal structure correspond to the outlets of the distributor 128 .
  • Fractals may also be 3-dimensional.
  • One 3-dimensional fractal element may be characterized as having four spokes radiating from a hub, with each spoke in fluid communication with paired exits. Such a fractal element may have exits located at the eight corners of an imaginary cube.
  • a second 3-dimensional fractal element may have three spokes radiating from a hub. Each spoke may terminate in an exit, or communicate with additional conduit structure to form an increased number of exits.
  • a distributor 128 or collector 136 may contain more than one fractal configuration. For example, one generation of “H” shaped fractal structures may feed a subsequent generation of “T” shaped fractal structures, and so on.
  • the total cross-section of successive generations of fractal structure is substantially the same as, or larger then, the total cross-section of the parent generation.
  • Such a cross-section arrangement helps to minimize fluid velocity at the inlet and outlet orifices.
  • it is desired that all conduit structures in a particular generation are hydraulically similar to promote evenly distributed flow throughout the generation.
  • FIG. 7 illustrates the same fractal propagation as in FIG. 6 but with an additional fractal iteration applied to the outside area. Such iterations are the key to this invention's progressive shrinkage of the height of the apparatus.
  • FIG. 7 only shows the peripheral area additionally iterated for illustrative purposes. The iterative procedure of course applies to the entire volume of the fractal distributor zone to distribute exit or collection points throughout the volume occupied by a distributor 128 or 136 . The number of additional iterations is only limited by manufacturing techniques.
  • a bed 132 of a given volume is configured with significantly reduced column height 144 (measured along the flow path of the traveling fluid, without regard to orientation) and a correspondingly increased cross sectional area (measured transverse the fluid flow path through the bed), as compared to a conventional bed configuration.
  • Use of the shallow bed configuration enables the processing of a fluid through a bed 132 which is reduced in height by at least 70% compared to a given conventional fluid process. In fact, there is practically no limit on the reduction of bed height which can be achieved by the practice of this invention.
  • those according to this invention are characterized by diameters significantly larger; typically at least double, their heights. Ratios of diameter to height in excess of 10:1 are practical, and ratios well in excess of 100:1 are also currently regarded as practical. As one example, the illustrated embodiment in FIG. 1 has a ratio of about 50:1.
  • diameter should be understood to mean “effective diameter;” that is, a dimension intermediate the major and minor axis of any such configuration.
  • the invention creates possibilities for cell construction using a wide range of normally unacceptable materials.
  • Fluid front overlap is reduced.
  • Typical examples of such benefits which can be obtained with this invention include a reduction of the band broadening which occurs in chromatography and the reduction of fluid overlap in other applications.
  • This invention enables the construction and operability of fluid processing with practically no limit on the “thinness” of the column bed.
  • the advantages of very low bed pressure drop and reduced linear velocity through the bed are therefore realized.
  • there is practically no limit on the reduction of the column height because uniform fluid distribution can be recursively improved.
  • a softening resin referred to as a weak cation exchange resin was used (Bayer CNP LF).
  • the resin regenerant was sulfuric acid (hydrogen form regeneration) and the exhaustion material for softening was approximately 15% DS “thin juice” obtained in the processing of sugar beets.
  • the feed material and regenerant are entirely conventional to weak cation thin juice softening.
  • a shallow cell was constructed with a diameter of 2 feet. Fractal distributors were used as mirror images for both the inlet distribution 128 and the outlet collection 132 . Flow was allowed for both the downflow and upflow directions.
  • the bed depth of the weak cation ion exchange resin was 6 inches.
  • the bed D:h ratio was 4:1 To demonstrate that a shallow bed could be operated without the prior art requirement of an over packed bed, 6 inches of void space 156 above the bed 132 was included in the cell design (see FIG. 3).
  • bed pressure drop is not needed to cause the required even fluid distribution.
  • bed pressure drop was reduced to only 1.5 psi compared with the conventional 50-80 psi. Therefore the instant apparatus operates at a bed pressure drop reduced by at least a factor of 30, compared to conventional devices. Even at a pressure drop of 5 psi across the bed, the instant device reduces processing pressure drop by at least an order of magnitude from that required by a conventional apparatus.
  • This invention can be applied over the entire range of fluid processing scales from very small scale applications to very large scale industrial use.
  • the reason for this is that the fractal structures used in combination with shallow cell/shallow bed design provide a continuing scaling function as application scale changes.
  • fractal type as in FIG. 6 with very small feature size was constructed using stereolithography.
  • the fractal was designed with final exit diameter of 0.015 inch.
  • the fractal was designed as 10 plates. The plates were then manufactured as a monolithic part.
  • Stereolithography is one technique which allows very fine feature size.
  • the shallow cell apparatus of this invention can be used in single cell applications, a key purpose of this invention is to use such cells in multi-cell configurations. Shallowing multi-cell processes will result in the same benefits of high productivity, cost reductions etc.
  • Examples of multi-cell configurations which will benefit from the replacement of conventional cells with the shallow cells of this invention include:

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US09/769,881 2000-01-27 2001-01-25 Shallow bed fluid treatment apparatus Abandoned US20010032814A1 (en)

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US10/867,968 US7390408B2 (en) 2000-01-27 2004-06-14 Shallow bed fluid treatment apparatus

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Cited By (12)

* Cited by examiner, † Cited by third party
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WO2007040967A1 (en) * 2005-09-30 2007-04-12 3M Innovative Properties Company A single pass method and apparatus for separating a target molecule from a liquid mixture
WO2007121751A1 (en) * 2006-04-24 2007-11-01 Jan Marcussen Double flow chromatography system
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EP1251926A4 (en) 2003-05-14
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US7390408B2 (en) 2008-06-24
WO2001054790A1 (en) 2001-08-02
EP1251926A1 (en) 2002-10-30
US20050000879A1 (en) 2005-01-06
AU2976901A (en) 2001-08-07
AU2001229769B2 (en) 2006-05-25
PT1251926E (pt) 2012-03-27
ES2379540T3 (es) 2012-04-27
CA2398235C (en) 2013-08-13
CA2398235A1 (en) 2001-08-02
BR0107842B1 (pt) 2011-07-12
ZA200205172B (en) 2003-09-26
BR0107842A (pt) 2002-10-22
DK1251926T3 (da) 2012-03-05

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