WO1993016786A1 - Appareil de fractionnement de fluide ameliore - Google Patents

Appareil de fractionnement de fluide ameliore Download PDF

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Publication number
WO1993016786A1
WO1993016786A1 PCT/US1992/001510 US9201510W WO9316786A1 WO 1993016786 A1 WO1993016786 A1 WO 1993016786A1 US 9201510 W US9201510 W US 9201510W WO 9316786 A1 WO9316786 A1 WO 9316786A1
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WO
WIPO (PCT)
Prior art keywords
fluid
columns
fractionating
mixture
rotor
Prior art date
Application number
PCT/US1992/001510
Other languages
English (en)
Inventor
Charles C. Hill
Theodore B. Hill
Original Assignee
Hill Charles C
Hill Theodore B
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from US07/660,177 external-priority patent/US5112367A/en
Application filed by Hill Charles C, Hill Theodore B filed Critical Hill Charles C
Priority to PCT/US1992/001510 priority Critical patent/WO1993016786A1/fr
Priority to JP50738692A priority patent/JP3269626B2/ja
Priority to EP92907872A priority patent/EP0627953B1/fr
Priority to AU14696/92A priority patent/AU1469692A/en
Priority to CA002130824A priority patent/CA2130824C/fr
Priority to DE69227922T priority patent/DE69227922T2/de
Priority claimed from CA002130824A external-priority patent/CA2130824C/fr
Publication of WO1993016786A1 publication Critical patent/WO1993016786A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0423—Beds in columns
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B01D2253/108—Zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/12—Oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40003—Methods relating to valve switching
    • B01D2259/40005—Methods relating to valve switching using rotary valves
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/45—Gas separation or purification devices adapted for specific applications
    • B01D2259/4533—Gas separation or purification devices adapted for specific applications for medical purposes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0446—Means for feeding or distributing gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption

Definitions

  • This invention relates to an improved apparatus and method for purifying a fluid product by removing certain components of a fluid mixture or contaminants from a source of a single fluid. Since this invention is effective in separation of gases and liquids, depending on circumstances, the term fluid will be used as much as possible. It is understood that the term includes gases arid liquids. Although focus is directed to the medical use as a respiratory support in the present embodiment, this invention is also useful in other situations where zeolites and sieve materials are employed, for example oil refinery procedures.
  • Air compressor Heat exchanger Air receiver or surge tank Two molecular sieve chambers
  • Product tank oxygen receiver
  • Adjustable flow control valve for oxygen product flow Connecting tubing and fittings to conduct fluid flows into and out of components
  • This invention encompasses improved apparatuses for fractionating a fluid mixture by pressure swing molecular adsorption. These apparatuses contain a plurality of adsorber columns and a chamber functioning as a purified product holding tank.
  • the heart of the apparatuses are unique, rotary distributor valve assemblies for sequentially pressurizing and exhausting each column. This allows pressurization of one of the columns while simultaneously purging the adsorbent medium in another of such columns.
  • This invention further encompasses improved processes for removing fluid components by selective adsorption of particular fluids from a stream of a mixture of fluids or a contaminating fluid component from a stream of a single fluid.
  • An incoming stream of a pressurized fluid mixture is sequentially distributed by means of rotating members of the rotary distributor valves of the alternative embodiments disclosed herein into a plurality of columns packed with an adsorbent which is selective for the fluid or the contaminant fluids to be removed.
  • the contaminants are retained by the adsorbent and the . desired product fluid is allowed to pass through ' .
  • Figure 1 depicts schematically a typical two-column adsorbent fractionating prior art system commercially available.
  • Figure 2 is a schematic representation of one embodiment of the entire fluid fractionator respiratory support system of the instant invention.
  • Figure 3 is a side elevation view of the apparatus which is the subject of Figure 2.
  • Figure 4 is a view taken on line 4-4 of Figure 3.
  • Figure 5 is an enlarged sectional view taken on line 5-5 of Figure 4.
  • Figure 6 is a sectional view taken on line 6-6 of Figure 5.
  • Figure 7 is a top plan view, partially cut away, of the rotor shoe, of the embodiment depicted in Figure 2;
  • Figure 8 is a sectional view taken on line 8-8 of Figure 7;
  • Figure 9 is a top plan view of the port plate of the embodiment depicted in Figure 2;
  • Figure 10 is a sectional view taken on line 10-10 of Figure 9;
  • Figure 11 is a side elevational view of an alternative configuration of the unit;
  • Figure 12 is a sectional view taken on line 12-12 of Figure 11;
  • Figure 13 is an enlarged sectional view taken on line 13-13 of Figure 12;
  • Figure 14 is a sectional view taken on line 14-14 of Figure 13;
  • Figure 15 is an underside view of the rotor shoe as taken on line 15-15 of Figure 13;
  • Figure 16 is a sectional view taken on line 16-16 of Figure 15; and Figure 17 is an enlarged sectional view taken on line 17-17 of Figure 12.
  • Figure 1 depicts schematically a typical small two- column oxygen concentrator commercially available for patient use. It can readily be seen from the schematic diagram that a typical medical oxygen concentrator is a complex machine, with a multitude of interconnected and interacting parts. Attendant with this manifold complexity is the prospect of decreased reliability, or the increased chance that some component will fail, rendering the entire apparatus incapable of performing its life-supporting function.
  • the cooling air in the exchanger is provided by a fan mounted on the compressor shaft, thereby, obviating the requirement of an additional motor and energy source.
  • an oxygen-rich fraction is tapped off through an outlet port 7 to the dispensing conduit, while the desorbed nitrogen is purged by the balance of the oxygen-rich product flow and leaves through an exhaust port 8.
  • the fluid fractionator in Figure 3, comprises a product holding tank 9 containing a cluster or array of adsorber columns within its housing, a rotary valve distributor 10 and a gear motor 11.
  • Figure 4 a view taken on line 4-4 of Figure 3, shows the arrangement of an array of columns 22 within the holding tank relative to the inlet 6, outlet 7 and exhaust 8 ports of the rotary distributor valve assembly, which is affixed to the holding tank by means of a clamp band 12. Twelve columns are shown in this case but there could be any number of two or more.
  • the rotary distributor valve depicted in Figure 5, which is an enlarged sectional view taken on line 5-5 of Figure 4, comprises a ported and channelled two-piece manifold 14 and a rotor 16 with a ported rotor shoe 18 and a cover plate 46, the rotor 16 being driven by a gear motor 11 ( Figure 3) at about two revolutions per minute, with the rotor 16 turning in circumferential ball bearing unit 17.
  • Conical disk or Belleville spring 35 urges cover plate 46 and rotor shoe 18 downward to secure them in position.
  • the rotor 16 and its associated components are enclosed by cover 21, which is attached to manifold 14.
  • the two-piece manifold 14 contains a top section 15 which is ported and channeled to take in a stream of fluid through the inlet port 6 and channel it through an air feed passage 33 into a centrally located inlet port 19 in the rotor shoe 18, and subsequently to channel the fluid mixture exiting the rotor shoe radially from a circular array of inlet ports located in the port plate 20 towards each column 22 of an array of columns arranged about the center of the manifold.
  • Each of these columns contains a bed of adsorbent material 24 (zeolite in this case) which is selective for a particular molecular species of fluid or contaminant.
  • the packed bed is held in place by a plate 26 at the bottom and perforated plates 27 at top and bottom with a spring 28 at the top.
  • the bottom plate has a pressure-dropping means such as a small orifice 60, the diameter of which is empirically determined, at the center of each column.
  • the bottom half of the manifold which is also an upper column header plate 30, affixed to the top half of the manifold by means of a clamp band 12, acts as a . cover for the channels and has the array of columns attached to its underside.
  • the channels in the manifold are sealed by a . gasket or sealing compound.
  • the port plate 20 Recessed into the top of the manifold, coaxial to the exit port of the air feed channel 33, sealed an immobilized by means of a slot and key, is the port plate 20 which contains a number of holes in an equally spaced circular pattern, equal in number and aligned with the circular distribution of entry ports of channels to individual columns in the manifold.
  • the manifold has a groove machined into its upper surface, ' just inside the port plate, which contains an air inlet rotary seal 32.
  • the port plate is made from a suitable hardened material.
  • the other major component of the rotary distributor valve is a gear motor-driven rotor 16 containing a ported rotor shoe 18, which slides over the rotor plate ( Figure 5, 6, 7, and 8 all depict various aspects of the rotor/shoe) .
  • the rotor shoe is made from material known in the art to be suitable for use with the hardened material comprising the port plate, and is held in position over the rotor plate by spring-loaded or pressure compensated means. Shown is a conical or Belleville pressure compensating spring to counteract supply pressure. An arrangement of small coil springs can also be utilized for this purpose.
  • One channel is a pressurizing channel or air feed passage 34 originating at the central fluid inlet port 19, and radiating into an arcuate slot 36 to simultaneously serve as a conduit into several of the circularly positioned ports in the port plate.
  • a pressurizing channel or air feed passage 34 originating at the central fluid inlet port 19, and radiating into an arcuate slot 36 to simultaneously serve as a conduit into several of the circularly positioned ports in the port plate.
  • Figure 5 a sectional view taken on line 6-6 of Figure 5, shows le relationship of the arcuate air feed port or slot 36 .- • _ " the rotor shoe 18 and the receiving ports 38 in the rt plate, as well as the air feed channels 31 to each o- ⁇ _he columns 22.
  • e wide exhaust port 40 collects refluxed fluid impurities desorbing and exiting from the ' columns, and channels them out through an exhaust outlet 8 ( Figure 5), through a "silencer" and into the atmosphere.
  • Figure 7 is a top plan view, partially cut away, of the rotor shoe. Several other features come into view here.
  • the desorbed columns are vented upward through the. exhaust slot 40, through a vent 42 in the rotor shoe cover plate 46, into the rotor void space, and out through the exhaust port 8 ( Figure 5) .
  • the third channel is a cross-port channel 44 which serves as a conduit between two columns which are in transition between the pressurizing and desorbing phases of a cycle. Its purpose is to quickly equalize pressure in columns transitioning between the adsorbing and desorbing cycles. This feature enhances product concentration at high product flow rates.
  • the purge flow rate is the rate at which the purging fluid flows countercurrent to adsorption during regeneration of the columns. There is an optimal purge rate for maximal removal of nitrogen during regeneration.
  • a very high purge rate causes the pressure within a bed to be greater than atmospheric, resulting in reduced desorption efficiency.
  • the cross-porting channel in the rotor shoe allows a pressure drop in the column bed before it enters the desorption cycle. This prevents a very rapid decompression and thus excessively high initial purge flow. This effect is easily measurable by simple instrumentation; however, its basis at the molecular level is not understood.
  • Figure 8 is a sectional view taken on line 8-8 of Figure 7, showing the routing of the pressurizing 34, cross-porting 44 and exhausting 40 channels in the rotor shoe 18.
  • Figure 9 is a top plan view of the port plate showing the circular location of ports of channels leading to each of the array of columns
  • Figure 10 is a sectional view taken on line 10-10 of Figure 9.
  • Figure 11 depicts an alternative embodiment of the apparatus of this invention, with a sectional view taken on line 12-12 thereof shown in Figure 12.
  • This latter view shows an array of adsorber columns similar to the columns 22 depicted in Figure 4.
  • twelve columns are the preferred number shown in the embodiment of Figure 12, but there could be any number of two or more. It should be noted, however, that a length to diameter ratio of greater than 6:1 for the.adsorber columns is preferred with the only limit on length being a practical one.
  • the rotary distributor valve depicted in Figure 13 which is an enlarged sectional view taken on line 13-13 of Figure 12, comprises a manifold 70 which is formed from one or more layers of aluminum, which layer or layers are pierced, and/or die formed or embossed and then, if a multiplicity of layers is used, sealed in a stacked configuration (by lamination or equivalent means) to form fluid channels.
  • a manifold 70 which is formed from one or more layers of aluminum, which layer or layers are pierced, and/or die formed or embossed and then, if a multiplicity of layers is used, sealed in a stacked configuration (by lamination or equivalent means) to form fluid channels.
  • Four layers of aluminum (74, 75, 76 and 77) are shown in Figure 13; it will be appreciated, however, that one or more layers of any lightweight, rigid, low density material (such as a-b-s resin plastic) may be used.
  • the rotary valve further comprises a rotor shaft 80 rotatably retained within bearing housing 81 and within rotor shoe 85. Rotation of rotor shaft 80 is permitted by the presence of O-ring 92 around its circumference. Rotor shaft 80 is driven by gear motor 90 via motor shaft 135 at about one revolution per minute. As depicted in Figure 13, said rotor shaft 80 is concentrically shaped above line 91 and eccentrically shaped below line 91. The eccentric shape is achieved by enlarging the lateral thickness of side wall 80A of rotor shaft 80 with respect to side wall 80B.
  • Rotor shoe 85 comprises a ported disc (similar in structure and composition to rotor shoe 18 depicted in Figure 7) with raised side walls 86 and 87 which define a circular chamber into which rotor shaft 80 is seated.
  • Rotor shoe 85 is driven by torque exerted by rotor shaft 85 when the latter is driven by gear motor 90.
  • Compression spring 93 assists in sealing the shaft and shoe, thus maintaining the seal even when the apparatus is not in operation and compensating for wear experienced by the shaft and shoe.
  • Use of this configuration to form a pressure balanced seal requires less torque to turn the rotor, and thus less energy to operate the system than required by prior art systems or the embodiment of Figures 3-10.
  • the pressure balanced seal between the rotor shaft and shoe is a function of the integrated pressure exerted on the surface of the rotor shoe between it and the rotor shaft during operation of the apparatus and the diameter of the rotor shaft.
  • the fluid pressure at fluid inlet port 109 at the start of adsorption multiplied by the diameter squared of the rotor shaft (below line 91) and by ⁇ /4 is equal the force exerted to form a seal between the shaft and shoe.
  • the shaft and shoe will remain sealed and balanced with respect to each other even if the fluid pressure at fluid inlet port 109 varies.
  • there is a passage (not shown) from port 109 through to the interface surface between rotor shaft 80 and rotor shoe 105 which serves to pressurize the interface to help maintain the pressure balanced seal.
  • said noise control design comprises muffler housing 100, having inner and outer surfaces preferably formed by a flexible plastic, which snaps, over manifold 70 to form a cover for the manifold and rotary valve distributor.
  • the noise control design further consists of pieces of acoustical foam or equivalent acoustical attenuating material placed within the apparatus as follows: at 101, said foam conforms topographically, in one or more pieces, to the inner surface of muffler housing 100. At 102, acoustical foam is seated vertically between bearing housing 81 and manifold 70.
  • Said foam 102 may be retained in place by a portion of layer 74 of manifold 70 formed to provide a stop 103 between foam 102 and port plate 105.
  • sound waves emitted by the operation of the rotary valve distributor escape from exhaust ports 113 and 114 in the rotor shoe into the annular air space 150 between the shoe and acoustical foam 102.
  • Those sound waves not dissipated by striking foam 101 and 102 eventually escape from slots 107 in the walls of muffler housing 100.
  • the noise control design would, therefore, be considered in the art as a reactive muffler.
  • Port plate 105 is similar in structure to port plate 20 of the embodiment depicted in Figure 5, except that, while the inlet ports therein to the adsorber columns (one port per column) may be of any shape, they are preferably in the shape of wedges and most preferably in a arched keystone shape which will circumscribe the orifices 160 leading into the columns 115 via air fed channels 116 ( Figure 14) . Wedge-shaped inlet ports are best depicted at 106 of Figure 14, which is a sectional view taken on line 14-14 of Figure 13. As in the embodiment of the apparatus shown in Figures
  • rotor shoe 85 comprises three sets of channels.
  • the first set of channels consist of pressurizing channels 110A and HOB which extend respectively and radially from central fluid inlet port 109 to symmetrical air feed ports 111 and 112 (while two air feed ports are shown, it will be appreciated that more than any number of two or more may be used as long as the ports are arranged in axial symmetry about inlet port 109) .
  • fluid travels through fluid inlet port 109 to air feed ports 111 and 112 through ports 106 in port plate 105 to air feed channels 116 (shown in Figure 14) which lead from each port 106 to an adsorber column (shown in sectional view in Figure 14 at 115) .
  • the second set of channels consist of at least two exhaust ports (113 and 114 in Figure 15) which will be equal in number to air feed ports 111 and 112 and will also be arranged with axial symmetry with respect to inlet port 109.
  • the desorbed columns are vented upward through exhaust ports 113 and 114, to annular air space 150 and eventually to the atmosphere via slots 107 in muffler housing 100 ( Figure 13) .
  • the third set of channels are at least one pair of symmetrical cross-port channels 118 and 119 (equal in number to air feed ports 111 and 112) . These channels serve to quickly equalize pressure between columns transitioning between the adsorption and desorption phases much in the same manner as does the single cross-port channel 44 depicted in Figure 7.
  • the number and symmetry of shape and size common to each set of channels avoids the preloading spring which results from the use of asymmetrical ports, where variances between the fluid pressure present at the air feed and exhausts ports may push the rotor shoe against the port- plate during operation.
  • the method of fractionation is as follows: compressed air enters the inlet port 6 of the manifold ( Figure 6) and is channeled through the air passage in the manifold 33 communicating with the rotor shoe 18 and then into the arcuate pressurizing slot 36 to enter sequentially into several ports 38 in the port plate as the rotor shoe 18 turns. As these ports become pressurized, the gas mixture enters, pressurizes and flows through each attached column 22 where the separation takes place.
  • the desired gas oxygen in this case, is free to move through the zeolite adsorbent bed 24 (e.g., similar to that provided by the molecular sieve division of UOP) , while the undesired gases and vapor (nitrogen plus C0 2 , CO, H 2 0) are retained, because of their molecular size and the relatively high pressure and low temperature, in the matrix of the adsorbent bed.
  • the purified desired gas product (oxygen) moves out of the column through a pressure-dropping means such as a small orifice 60 or a fluid porous plug in the bottom of the column and into the circumscribed product tank 9.
  • a relatively small portion of the oxygen is tapped off by the distribution system conduit at the outlet port 7 ( Figure 6) for use by the patient, and another, relatively large, portion enters the columns in the opposite bank, which are under nearly atmospheric pressure, through a corresponding small pressure dropping/flow restricting orifices in the bottom to reflux through the bed in a direction opposite to gas flow during pressurization.
  • the amount of product used to purge'versus the amount delivered by the distribution system can vary, depending on the degree of product purity desired.
  • This backwash of product gas at pressure lower than the adsorbing cycle removes the contaminant embedded in the zeolite matrix, in this case nitrogen, and flushes it out through the top of each column into the manifold 14, the port plate 20 and through the rotor shoe 18 and exhaust outlet 8 into the atmosphere via a silencer or muffler.
  • the tapped oxygen-rich product gas then moves within a dispensing conduit 46 through a manually controlled valve 50 with a flow meter, through a final filter (HEPA) 52 and to the dispensing terminus.
  • HEPA final filter
  • the method of fractionation is as follows: compressed air enters the manifold from inlet conduit 120 through inlet port 121 ( Figures 14 and 17) and is channeled through channel 71 communicating with the rotor shoe 85 via central fluid inlet port 109. The air then passes through radial channels 110A and HOB to inlet ports 111 and 112. As the rotor shoe turns over port plate 105, inlet ports 111 and 112 will each become aligned with an equal plurality of wedge-shaped ports 106, thus allowing the- ir to enter the columns 115 via air feed channels 116 corresponding with each plurality of ports 106 served respectively by inlet ports 111 and 112. Adsorption occurs within the columns as described above.
  • Product tank 130 differs from product tank 9 ( Figure 5) in that tank i30 is smaller in volume and does not surround columns 115 except at-their distal ends; i.e., opposite manifold 70.
  • This smaller product tank (vis-a-vis product tank 130 [Figure 11]) reduces the overall weight of the system.
  • the limits on reduction of the size of product tank 130 are practical ones, principally dictated by storage needs and the volume required to regulate the output pressure of the system sufficiently well to reduce the need for a pressure regulator.
  • Product is tapped for use by the operator or patient via outlet conduit 125.
  • the system is then purged as described above with respect to the method used with the apparatus depicted in Figures 3-10.
  • the cycle profile is such that each column is pressurized for approximately 12.5 seconds, equilibrated for 2.5 seconds, and desorbed for 12.5 seconds and re-equilibrated. This profile of the cycle is obtainable only when the intake and exhaust slots in the rotor shoe are equal in size, and service an equal number of columns.
  • the profile can be altered as desired by varying the size of the respective inlet and exhaust ports. This is a desirable feature which cannot be put into effect in any of the prior art mechanisms.
  • This cycle is sequentially and continuously established for each column. This mode of operation produces a relatively constant flow of product, improving with a greater number of columns, eliminating the need for a pressure reducing regulator.
  • the average product outlet pressure is nearly constant and about twice the regulated delivery pressure of prior art fractionators.
  • the column length may be short, even with a large length:diameter ratio which is essential for effective adsorption separation.
  • the large number of columns and the rotary distributor valve result in a quasi steady-state gas flow through the compressor and other components which produces a number of advantages and system simplifications.
  • the invention permits optimization of the adsorption cycle by providing the possibility of employing unequal times for the adsorption and desorption phases of the cycle.
  • Prior art two chamber systems are inherently bound to equal times.
  • Another notable advantage of the invention is the elimination of many components which are necessary in the prior art, thereby, reducing size, weight and the amount of maintenance, concomitantly increasing reliability and maneuverability for the ambulatory patient. These eliminated components include: Air receiver or surge tank
  • adsorbent material utilized in this embodiment is a synthetic zeolite
  • this invention should not be construed as restricted to its use. It is understood by those well versed in the art that many other configurations are possible while employing the rotary distributor concept, which are within the spirit and scope of this invention.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Of Gases By Adsorption (AREA)

Abstract

Un appareil amélioré pour fractionner des mélanges de fluides, tels que l'air, par adsorption moléculaire à oscillation de pression, utilise une soupape de distribution rotative (10) et un alignement de colonnes d'adsorption (22). Selon un mode de réalisation, ces colonnes ( 22) sont contenues à l'intérieur d'un réservoir (9) de produit, ou, selon un autre mode de réalisation, elles sont fixées à un réservoir (130) de produit. La soupape (10) est actionnée en séquence pour produire un écoulement pratiquement à l'état stable, permettant d'optimaliser les cycles d'absorption/de désorption, et de supprimer la plupart des soupapes, des interrupteurs et des conduits généralement requis.
PCT/US1992/001510 1989-11-20 1992-02-28 Appareil de fractionnement de fluide ameliore WO1993016786A1 (fr)

Priority Applications (6)

Application Number Priority Date Filing Date Title
PCT/US1992/001510 WO1993016786A1 (fr) 1989-11-20 1992-02-28 Appareil de fractionnement de fluide ameliore
JP50738692A JP3269626B2 (ja) 1992-02-28 1992-02-28 改良された流体分別装置および方法
EP92907872A EP0627953B1 (fr) 1992-02-28 1992-02-28 Appareil de fractionnement de fluide
AU14696/92A AU1469692A (en) 1992-02-28 1992-02-28 Improved fluid fractionator
CA002130824A CA2130824C (fr) 1989-11-20 1992-02-28 Appareil ameliore de fractionnement de fluides
DE69227922T DE69227922T2 (de) 1992-02-28 1992-02-28 Fluidumfraktioniervorrichtung

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US43878689A 1989-11-20 1989-11-20
US07/660,177 US5112367A (en) 1989-11-20 1991-02-25 Fluid fractionator
PCT/US1992/001510 WO1993016786A1 (fr) 1989-11-20 1992-02-28 Appareil de fractionnement de fluide ameliore
CA002130824A CA2130824C (fr) 1989-11-20 1992-02-28 Appareil ameliore de fractionnement de fluides

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WO1993016786A1 true WO1993016786A1 (fr) 1993-09-02

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6372026B1 (en) 1998-02-19 2002-04-16 Teijin Limited Apparatus for producing oxygen enhanced gas from air
US8016264B2 (en) 2006-05-02 2011-09-13 Teijin Pharma Limited Rotary-valve and adsorption separation system
US8016925B2 (en) * 2004-10-12 2011-09-13 Mccombs Norman R Mini-portable oxygen concentrator

Citations (13)

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DE737929C (de) * 1938-12-04 1943-07-29 Bamag Meguin Ag Adsorptionsanlage zur Rueckgewinnung von Loesemitteln
US2759560A (en) * 1953-03-02 1956-08-21 Jefferson Lake Sulphur Co Method of removing water vapor and recovering condensable hydrocarbons from natural gas under high pressure
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