JP2000501336A - Shear action localized filtration system - Google Patents

Abstract

(57) Abstract: A stack of rapidly rotating membrane packs (32) and a stack of stationary separation elements (36A, 36B) with the membrane pack sandwiched to leave a small gap (40A, 40B) therebetween. There is provided a filtration device of the type that includes the advantages of both a series connection system and a parallel connection system. Feed conduits (82) connect the radially outer ends (110) of the gaps to carry feed fluid into and out of each gap. The rapidly rotating membrane pack causes a radially outward flow near its surface, which results in a radially inward flow (102) near the surface of the stationary element and radially through each gap. Causes a fluid flow inward and then outward. The stationary element has openings (131-138) to equalize the pressure on both sides and promote fluid shearing at the membrane surface. An accumulator (140) is coupled to the feed inlet (12) to maintain the feed fluid pressure during an abnormal drop in feed fluid pressure for the time required to stop rotation of the stack of membrane packs.

Description

DETAILED DESCRIPTION OF THE INVENTION Shearing localized filtration system Background of the Invention The feed fluid, such as wastewater, can be separated into a permeate, such as pure water, passing through the membrane and a concentrate containing water with a high particle concentration. For such separation, a stack of membrane packs in a container may be used. Clogging of the membrane pack due to accumulation of particles on the surface that plug the pores of the membrane can be caused by rapid rotation of the membrane pack as described by Croopnick in U.S. Pat. No. 4,025,425. It can be reduced. Clogging can be further reduced by placing a stationary separation element between the pairs of membrane packs, causing turbulence in the gap between the rotating surface of the membrane pack and the stationary surface of the separation element. Here, if the membrane pack has large pores (large widths in microns), this may be referred to as a filter pack, but Applicants will use the term membrane pack herein for both. The turbulence enhancing separation elements between the membrane packs should be relatively thin so as to take up less space, but not in contact with the rapidly rotating membrane pack. Otherwise, this separation element will be destroyed. It would be desirable for the separation element to be designable with maximum strength against deflection while minimizing conditions that can cause its deflection. Conventional filtration structures direct the feed fluid in series through the gap. For example, if there are 50 membrane packs and corresponding stationary elements to make 100 gaps, fluid can flow in a series tortuous path through the 100 gaps. Such a serial flow has the advantage that the feed fluid travels along a long path in contact with the surface of the membrane pack to remove a significant portion of the filtrate. However, the drawback of such a serial flow is that the feed fluid is not homogeneous because the particle concentration in the feed fluid can increase many times between the upstream and downstream ends of the feed fluid path. There is. Also, particularly with highly viscous liquids, large pressure drops can occur along long paths due to friction on the moving feed fluid. With such a large pressure drop, only a small portion of the total feed fluid path will have optimal feed fluid pressure (for permeate flow that maximizes flow through the membrane while minimizing clogging). It can be not. Rarely does the supply fluid flow in parallel across all gaps. This is because the short path length requires the fluid to be cycled back in order to flow again, resulting in high pressure losses. A filtration system that allows the feed fluid to flow along a long path that contacts the membrane surface while maintaining the feed fluid primarily homogenous in pressure and particle concentration would be beneficial in filtering a variety of fluids. Summary of the Invention According to one embodiment of the present invention, there is provided a filtration system in which a stack of rotatable membrane packs is spaced by a separation element, leaving a gap through which feed fluid travels, thereby facilitating filtration. Is done. The filtration system is operated such that the feed fluid is flowed from a substantially stationary separation element into a conduit connecting the radially outer edges of the gap separating the rotating membrane pack. Some portion of the feed fluid flows predominantly radially inward along an inboard path adjacent to the stationary element, and flows predominantly radially outward along an outboard path adjacent to the rotating membrane pack and primarily circulates. A flow is created along each gap. Some portions of the fluid that have moved radially inward and outward along the path travel through the supply conduit to another gap, while other portions return along the inward path to the same gap. The feed fluid moves to and from each gap and along a long path as it flows radially inward and outward along each gap, but the fluid in each gap is displaced by the feed conduit. A substantially homogeneous feed fluid is still maintained because it is constantly mixed with fluid from other gaps. As the feed fluid moves through the gap, the permeate of the feed fluid passes through the membrane of the membrane pack and exits the device. Centrifugal forces and shearing action (difference in fluid velocity near the pack surface) minimize the accumulation of particles on the membrane surface that would clog pores in the membrane. The stationary separating element has openings to leave the spokes, which helps to create a shearing action and equalizes the pressure on both sides of the element. Preferably, an accumulator is connected to the supply conduit, such as at a supply inlet. Such an accumulator ensures that the supply fluid pressure can only be reduced gradually and prevents rupture of the membrane when the membrane pack stops rotating in the event of a loss of supply fluid pressure. The novel features of the invention are set forth with particularity in the appended claims. The invention will be best understood from the following description when read in connection with the accompanying drawings. BRIEF DESCRIPTION OF THE FIGURES FIG. 1 is an isometric view of a rotary filtration device constructed in accordance with one embodiment of the present invention. FIG. 2 is a sectional side view of the apparatus of FIG. FIG. 3 is a view taken along line 3-3 in FIG. FIG. 4 is a cross-sectional view of a portion of the apparatus of FIG. 2 taken at line 4-4 in FIG. FIG. 5 is an enlarged view of a part of the apparatus of FIG. FIG. 6 is an enlarged view of a part of the apparatus of FIG. FIG. 7 is a view taken along line 7-7 of FIG. 3, but with exaggerated axial dimensions, the plus (+) sign indicates flow to paper, and the circle indicates flow from paper. . FIG. 8 is a partial side sectional view of a rotary filtration device constructed according to another embodiment of the present invention. Description of the preferred embodiment FIG. 1 shows a rotary filtration device 10 having a feed fluid inlet 12 for receiving a feed fluid. The feed fluid generally comprises a liquid and particles within the liquid having a size in the micron range (mean diameter less than 10 microns) or a size in the submicron range. The apparatus separates the feed fluid into filtrate or permeate flowing from permeate outlets 14, 16 and concentrate flowing from outlet 20 (or from inlet 12 in the case of batch processing). The retentate contains a liquid with a high particle concentration and remains after much of the permeate in the original feed fluid has been removed. The apparatus includes a rotor 22 that is inside a sealed container 24. A motor 26 is coupled to the rotor and causes it to rotate rapidly with respect to shaft 28. As shown in FIG. 2, rotor 22 includes a stack 30 of axially-spaced membrane packs 32 (in a direction X parallel to the axis) within a container. The device also includes a stack 34 of plate-like separation elements 36. The separation element 36 is stationary and is positioned such that the separation element 36 is between each pair of membrane packs 32. This leaves a gap 40 between each surface of the membrane pack and the adjacent surface of the separation element. The gap extends radially (parallel to radial direction Y) in that it has a large radial Y dimension and a small axial X dimension. In particular, FIG. 2 illustrates a first membrane pack 32A and a second membrane pack 32B, separation elements 36A and 36B, and a first gap 40 and a second gap 40B on either side of the first membrane pack 32A. Show. FIG. 2 shows that the membrane pack 32 is mounted halfway along a hollow shaft 50 to form a filtrate conduit 52. The filtrate conduit extends the entire length of the shaft and forms filtrate outlets 14, 16 at both ends of the shaft. The shaft is rotatably mounted on bearings 54, 56, 58, with a platform, indicated at 59, for supporting the lower bearing and the upper bearing supported on the container 24. It is possible to rotatably support the rotor on a bearing assembly that includes a single bearing. The membrane pack 32 has a radially inner end 60 and an outer end 62. The inner end 60 is attached to the shaft and the outer end 62 is not fixed and is therefore not supported. The separation element 36 has a radially inner end 64 and an outer end 66. Outer ends 66 are attached to a group of stays 70 and are spaced by spacers 72. The radial inner end 64 of the separating element is not fixed and is therefore not supported. As shown in FIG. 3, each of the separation elements 36 has a through opening 131-138 leaving a spoke 141-148. The opening extends radially further (away from axis 28) than the perimeter 150 of the membrane pack. This leaves a space 152 in the radially outer portion of the opening through which the feed fluid can move. Also, the radially outer end 66 of the separation element is radially spaced from the sidewall 80 of the container 24. This leaves additional space 154 along which the feed fluid can move. The spaces 152, 154 form the supply conduit 82, which is primarily donut-shaped (with the perimeter of the spacer element therein). As shown in FIG. 4, the cross-sectional area of the supply conduit 82 as seen in the cross-sectional view of FIG. As a result, the feed fluid tends to be substantially homogeneous in the filtration device due to the substantially uniform pressure of the feed fluid and the substantially uniform solids concentration in the liquid of the feed fluid. It is. Here, the radial inner ends 60 of the membrane packs are spaced by sealing spacers 84. The filtrate flows radially inward along each membrane pack, through holes 86 in the rotor shaft, and along the permeate conduit 52 of the shaft. FIG. 5 shows the flow of fluid in a gap, such as 40A and 40B, and along a supply conduit. Feed fluid 90 fills feed conduit 82 and gaps such as 40A, 40B until the membrane pack, such as 32A, begins to rotate. As the membrane pack 32A rotates rapidly, fluid adjacent to the membrane pack surface 92 rotates with the membrane pack. Such rotation creates a centrifugal force, which forces the feed fluid present adjacent surface 92 radially outward along an outward path 94 (including the circumferential component in the direction of rotation of the membrane pack). Move. The radially outward flow along the outer path 94 reduces the pressure at the radially inner end 100 of the gap, thereby creating a radially inward flow of the feed fluid along the inner path 102. The result is a circulating flow of feed fluid along each gap. This circulating flow causes fresh feed fluid from feed conduit 82 to flow repeatedly over membrane pack surface 92. The feed fluid permeate enters the porous backsheet 106 of the membrane pack through the membrane 105 or other filtration element, travels along the membrane cross-path 104, and travels in an inward direction 108 to the center of the pack. From which the permeate is removed. Note that the membrane or filtration element can be a polymer membrane, a screen (woven or matted or etched), a porous ceramic, a sintered metal, or a structure that allows only small particles or molecules to pass through. Applicants use the term "membrane pack" for all such elements. Typical treatments include dialysis, electrodialysis, reverse osmosis and filtration of various sizes. Applicants' system is particularly beneficial for microfiltration and for ultrafiltration, but could also be used for nanofiltration, and perhaps even reverse osmosis. At the radially outer end 110 of the gap, fluid traveling along the outer path 94 is mixed with the feed fluid, and some (at least 1%) of the fluid traveling along the outer path 94 is indicated by the path 112. And some (at least 1%) move to the supply conduit as shown by path 114. Fluid that does not recirculate in the same gap 40A can move along the supply conduit 82 to another gap, such as 40B. At the inner end 100 of the gap, much of the fluid flows back along the gap in a loop indicated by 120. Although some of the fluid flows in the path 122 between adjacent gaps, such as 40A and 40C, the radially inner ends of both gaps 40A, 40C are subjected to substantially the same pressure, so that There is little flow. FIG. 6 shows the velocity profile of the feed fluid flowing along gap 40 in the circumferential direction (radial velocity component not shown) by the length of the arrow. The circumferential direction is perpendicular to the radial direction and parallel to the movement of the membrane pack surface. The path of 93A is very close to the membrane pack surface 92 and the fluid travels at approximately the same speed as the rotating surface 92. The speed of path 93 is much lower than the speed of 93A, and the difference component 93D tends to flush particles 111 from the surface 92 of the membrane pack. This phenomenon is referred to as localized shearing, which tends to push particles away from the surface. For a given velocity of the surface 92 relative to the stationary separation element surface 113 of the separation element, the magnitude of such shearing action depends on the thickness 116 of the gap. The smaller the thickness 116, the greater the localized shearing effect, or the ratio of the speed difference 93D to the distance 118 along the gap. Applicants prefer to make the gap 116 as small as possible, but the surfaces 92, 113 must not touch. This is because this can cause damage to the membrane pack. Applicants can obtain a gap thickness 116 of about 2 millimeters in a stack of dozens of membrane packs without causing damage to the membrane packs. In addition to the velocity difference per unit distance, small gaps lead to large turbulence at the surface, and such turbulence near the surface 92 tends to flush away particles that might otherwise block pores in the membrane. Here, the large circumferential fluid movement at 93A and 93 leads to fluid near the membrane pack flowing outward in the radial direction. Thus, by connecting the feed conduit to the radially outer end of the gap between the membrane pack and the separation element, applicant causes recirculating flow through each gap, where: The feed fluid moves radially inward near the surface of the separation member and radially outward near the surface of the filter pack. Feed fluid, which moves primarily radially outward near the outer end of the gap, flows into the feed conduit and recirculates. Since the fluid circulates through many gaps, perhaps several times, applicants have in series a gap in which each amount of fluid moves along many membrane pack surfaces to remove a significant portion of the filtrate from the feed fluid. Get the benefits of connecting. Applicants have avoided the disadvantages of series connection, which is that the pressure is approximately the same everywhere and the mixing of the fluid near the outer edge of the gap is such that the feed fluid has almost the same solids concentration everywhere. In connection, this is because the system of the present invention produces a substantially homogeneous fluid in the device. As mentioned above, the substantially uniform pressure in the system allows the applicant to apply optimal pressure to the feed fluid. For example, in some situations, a pressure of 40 psi provides a high flow rate of permeate to the membrane pack while minimizing plugging of the membrane pack, but a pressure of 80 psi can cause plugging and a pressure of 20 psi can lead to a low permeate flow rate. . The optimum pressure depends on the solids concentration. Applicants can adjust the rate at which the concentration is reduced based on the permeate flow in order to vary the solids concentration to obtain a significant permeate flow rate while minimizing membrane clogging. As shown in FIG. 3, applicants have created openings 131-138 so as to leave spokes 141-148 forming walls on both sides in the circumferential direction (perpendicular to the radial line) of each opening. It is preferred to configure each separating element 36 provided. One of the advantages of the opening is that it provides the same pressure on both sides 160, 162 of the element. Applicants have noted that for a system using a 410 mm diameter membrane pack, the membrane pack has a small thickness, such as 8 mm, the spacer element has a small thickness, such as 6 mm, and each gap is I prefer to have a thickness such as 3 mm. The small thickness of the spacer element will cause the location above it to flex axially if there is a slight pressure difference between its two sides. Any such axial deflection that results in direct contact between the spacer element and the rapidly rotating membrane pack will cause the membrane pack to break. At least one opening occupying at least 10% of the area of each spacer element, and at least 10% of the area of each sector and the separating wall (eg, spokes) in each sector, for each virtual 90 ° sector 164 of the separation element. Applicants avoid such pressure differences. When the membrane pack rotates so that the portion shown in FIG. 7 moves in the circumferential direction of arrow 170, the supply fluid at 172 adjacent to pack surface 92 also moves in the circumferential direction. Applicants configure each spoke, such as 144, 145, with tips 174 designed to interfere with circumferential fluid movement. The result is a large change in fluid velocity over a short distance near the membrane pack surface, which helps to flush the particles. The flow near the membrane pack is usually turbulent, and the separation is called the "turbulence generator". Of course, if there is no separation, the fluid between the pair of membrane packs will soon rotate with the pack. With a separation, most fluids are stationary or only spin slowly, which causes a sudden change in velocity near the membrane pack. The cross-section of each spoke, such as 144 in FIG. 7 (with exaggerated thickness), is selected such that the spokes are automatically centered. That is, when the spokes approach the membrane pack surface 93 where the spokes are located, the reaction between the spokes and the fluid moving in the circumferential direction 170 will move the spokes away from the membrane pack surface 93. Applicants have experimented with spacer elements having various numbers of spokes. An element as shown in FIG. 3 with eight spokes was found to be the best in the test. The element with four spokes performed almost identically, though not completely. Preferably, the number of spokes is at least 4 and not more than 16. The radially inner ends of the spokes are joined by a continuous 360 ° hub 180. The spokes' radially outer ends are preferably joined by a continuous rim 182, but this is not necessary. The openings and spokes can be angled from a radial direction. The membrane pack is rotated quickly enough such that large centrifugal forces and large shearing effects occur to prevent membrane clogging. A 410 mm diameter membrane pack is rotated at at least 200 rpm, usually about 760 rpm to 1000 rpm. At 200 rpm, the average surface speed (at 0.4 inches from the axis) is about 2 meters per second. Thus, the system operates at an average membrane pack speed of at least 2 meters per second and a pack peripheral speed of at least 4 meters per second. The most effective rotational speed for a membrane pack typically produces a centrifugal force that increases the pressure by at least 20 psi (140 kPa). The rotary filtration device 10 (FIG. 1) may be operated in a batch process, a continuous process, or a combination thereof. In batch processing, a feed fluid having a predetermined solids concentration, such as 200 ppm (parts per million), is pumped into a container. The inlet valve 220 and outlet valve 221 are closed. The pump 222 may be connected to a recirculation conduit 230 to maintain a more uniform particle concentration, such as by splitting the donut-shaped feed conduit 82 of FIG. 3 into two parts, one part above and the other. Can be achieved in the container 24) (by pumping the fluid down in the section). Inlet 12 and outlet 20 form an axially spaced location of the supply conduit, and recirculation conduit 230 is external to the supply conduit. A sensor 224 is connected to the container to sense the particle concentration. The motor 26 is activated so that the rotor 22 rotates at a predetermined speed and the permeate is constantly withdrawn from the feed fluid, while the particle concentration in the feed fluid increases. The sensor 224 senses this and controls the pump 222 to change the pressure of the feed fluid for optimal conditions (high permeate flow to the membrane pack and low clogging of the membrane pack surface), Further, the motor 26 can be controlled so as to change the rotation speed of the rotor. In a continuous process, the feed fluid may flow from source 232 to feed fluid inlet 12 at a slower rate but continuously. The concentrate flows out of outlet 20 for use or future processing. It is noted that in some prior art filtration systems, particles of the filtrate have been mechanically accumulated to a large thickness (thickness of multiple particles) on the filter or membrane surface. In the present invention, only "clogging" which is a chemical phenomenon occurs, not "accumulation" which is a mechanical phenomenon. In clogging, solutes (particles) are absorbed or adsorbed to the membrane by affinity to the point where permeate flow through the membrane is significantly reduced. Clogging can occur at and below the surface. For example, very small particles can adhere to the wall of the membrane pore until the particles close the pore and stop permeate flow, causing clogging. The thickness of the particles clogging the membrane is less than one-tenth of the gap width, at which time cleaning must begin. The present invention can prevent any accumulation and reduce the rate of clogging. Choosing the right membrane material for a particular application is very important in reducing the plugging rate. Once clogging has occurred, the membrane may be cleaned, such as by using a chemical to dissolve or release the particles that have adhered to the interstices of the membrane. By measuring the flow rate of the permeate, the degree of clogging can be determined and when cleaning is necessary. Applicants prefer to keep the accumulator 240 (FIG. 1) connected to the supply conduit 80 at any time. The accumulator ensures that the pressure of the feed fluid changes only slowly, despite possible interruptions in the feed or other phenomena that can cause the feed fluid pressure to drop rapidly. If the feed fluid pressure drops abruptly but the permeate pressure in the membrane pack drops only slowly, a higher permeate pressure in the membrane pack could rupture the thin membrane. The accumulator 240 is of a conventional type and resides in a container 244, a membrane, bellows or piston separating the container into an air chamber 246 containing air under pressure and a liquid chamber 248 containing liquid under the same pressure. Including a dividing member 242. Any other means of maintaining feed fluid pressure is used, such as a valve connected to a high pressure liquid source, such as a city water main, that opens only when a rapid pressure drop is sensed. You may be. If the accumulator has to pump fluid for more than a fraction of the time, such as when it is almost empty after being full, the motor is preferably automatically powered off. The rotor should stop substantially from perhaps 700 rpm for a period such as 8 seconds, and the fluid pressure should be maintained for perhaps 6 seconds. FIG. 2 shows that the permeate exits the device at 14 and 16 through the ends of the shaft in opposite directions A, B. For high filtrate flows, smaller shafts and seals such as bearings 54, 56 and 58 and 59 'are used, reducing costs. FIG. 4 shows that holes 250 are formed at the radially inner end of the membrane pack to allow the feed fluid to flow primarily axially from one inner end gap to another. However, the flow through such holes is very small, and providing such holes could increase the cost of the membrane pack due to the need to seal off the movement of the feed fluid to the permeate. FIG. 8 shows a portion of another rotary filtration device 260 similar to FIGS. 1-6, except that the separation elements 262 between adjacent rotary membrane packs 264A, 264B also form a membrane pack. That is, each separation member 262 has a membrane sheet 266 and a flow sheet 268 for removing permeate. The permeate passing through the membrane pack separating member 262 passes through a hole 270 in the hollow binding member 272 corresponding to the binding member 70 in FIG. 2 for removing the permeate. In one system designed by the applicant, the membrane pack has a diameter of 16 inches (40 cm), the gap 40 is 3 mm thick, and other dimensions are relative to the diameter as shown in FIG. there were. In one application, aluminum oxide particles sized 0.5 microns or more (originally used for dyes) were removed from the brine and dissolved solids waste stream. The aluminum oxide particles were concentrated from 4% to 20% of the volume of the stream by removing the brine and dissolved solids that make up the permeate of the waste stream. Larger particles have been previously removed by settling and sieving so that the largest particles do not have a diameter greater than about 10 microns. The feed fluid is initially maintained at a pressure of 40 psi (270 kPa) and the membrane pack is rotated at 800 rpm. As the concentration increases, the pressure can be kept constant or slightly increased. Thus, after the concentration increases, the speed is increased to 1000 rpm and the pressure is increased to 50 psi (340 kPa). Thus, the present invention provides a filtration system in which the feed fluid moves through an axially thin gap between the membrane pack and the separation element. This system benefits from the series connection of gaps and long flow paths along the membrane surface, while avoiding the disadvantages of widely varying pressure and particle concentrations. The system includes a supply conduit that connects the radially outer ends of the gaps to each other to flow fluid through each gap in a loop to promote uniform fluid flow in the system. The separating element preferably has a through opening to leave a spoke. While particular embodiments of the present invention have been described and illustrated herein, it will be appreciated that modifications and changes will readily occur to those skilled in the art and, therefore, the claims extend to such modifications and equivalents. Should be interpreted as

[Procedure amendment] [Submission date] March 8, 1999 (1999.3.8) [Correction contents] The scope of the claims 1. A container (24) having a plurality of stationary elements, on a shaft (28), A shaft (50) extending into the container and attached to the shaft; At least having opposed surfaces and an interior for carrying filtered fluid. And one membrane pack (32) and the filtered fluid coupled inside the pack. An outlet (52) for carrying away said stationary element (36). Inside the container beyond the opposite faces of the rack, between which the radial inner end (1 00) and a gap (40) forming a radially outer end (110). Further comprising connecting the shaft and the at least one membrane pack to the shaft; A motor (26) for rotating relative to a shaft, and coupled to and provided within said container; A feed inlet (12) for flowing a feed fluid, the filter comprising:   The supply inlet (12) formed in the container and the radial direction of the gap; Characterized by a supply conduit (82) connected to the outer end (110) of the , The supply conduit extends around the outer end of the gap, and If the body goes from the location of the supply conduit to the gap and vice versa From the gap so that it can flow to the location of the supply conduit. A device that connects the radial outer ends together. 2. The first stationary element has an element surface adjacent to a surface of the membrane pack. And the element surface has a plurality of recesses,   The element surfaces are four virtual fans each defining an angle of 90 ° with respect to the axis A plurality of recesses, each of the plurality of recesses including a recess in each of the sector portions; 2. The filtering device of claim 1, wherein the recess occupies at least 10% of the area of the sector. . 3. The element surface has a plurality of mainly radially formed between the recesses. 3. The filtering device of claim 2, wherein the filtering device has spokes that extend and extend radially. 4. Four recesses extending along most of the radius of the first element surface Form 16 mainly radially extending spokes, said spokes being said The filtering device according to claim 2, wherein the filtering device has a surface that is on the first surface of one element. . 5. The at least one membrane pack includes a stack of membrane packs and the stationary element The element comprises a stack of elements, each element being between a pair of said membrane packs. The filtration device of claim 1, comprising: 6. A sealed container (24) having a supply inlet (12);   A shaft (50) on the axis (28) and extending into the container;   At least one membrane pack (3) attached to the shaft and within the container 2) wherein the membrane pack has opposing surfaces; and   So as to leave a gap between each side of the membrane pack and one of the elements, A pair of stationary elements (36) in the container on both sides of the membrane pack;   Connected to the shaft to rotate it and the membrane pack about the axis Including a motor,   At least a first said element has a first surface adjacent to a surface of the membrane pack. And wherein the first surface is directly opposite the first surface of the membrane pack. A plurality of recesses (131-138) occupying at least 10% of the area of the surface,   The first surfaces of the first turbulence generator each define an angle of 90 ° with respect to the axis. Have four virtual sectors, and the plurality of recesses have a small area of the sector. A filtering device comprising, in each of said sectors, a recess occupying both 10%. 7. The first element comprises a plurality of mainly radially formed grooves between the recesses. The spokes (141-148) extending in the radial direction and extending in the radial direction. 3. The filtration device according to item 1. 8. While maintaining a pair of substantially stationary elements on each side of the membrane pack, At least one membrane pack in a sealed container having a Rotating the element so that the element faces the pack surface. And the distance between them is between the first said pack surface and the first said first edge. Forming a pair of gaps, including a first gap with the element surface; The feed fluid to be separated into a permeate and a concentrate is placed in the gap so as to enter the gap. A method for operating a rotary filtration device, comprising supplying to a container. hand,   An inward position within the first gap and adjacent to a location on the first element Flowing some of the feed fluid at least partially radially inward along the path. And adjoining the first element and within the first gap. Substantially all of the feed fluid is radially inward rather than radially outward. Flow, and   Permeate some of the permeate from the feed fluid to and from the membrane pack The first pack being in the first gap while flowing to a liquid conduit; Feeding said at least partially radially outward along an outer path adjacent to the surface Flowing some of the fluid, substantially adjacent to the first pack surface. All feed fluid flows radially outward rather than radially inward. In addition,   Flowing radially inward along the inward path in the first gap; A portion of the feed fluid flowing radially outward along the Flow to a supply conduit that connects to the supply conduit. 9. The supply conduit is within the container and extends at least partially in the axial direction Present radially outward from said membrane pack,   Flowing the feed fluid at least partially axially along the feed conduit From the supply conduit to each of the gaps and from each of the gaps 9. The method of claim 8, comprising flowing a supply fluid into the supply conduit. . 10. Starting a process to clean the membrane pack;   Prior to the step of initiating the process to clean the membrane pack, Of the thickness of the gap between each of the element surfaces and an adjacent one of said element surfaces Allowing the particles of the feed fluid to accumulate on the pack surface only to a thickness of less than one part 9. The method of claim 8, comprising the steps of:

────────────────────────────────────────────────── ─── Continuation of front page    (81) Designated countries EP (AT, BE, CH, DE, DK, ES, FI, FR, GB, GR, IE, IT, L U, MC, NL, PT, SE), OA (BF, BJ, CF) , CG, CI, CM, GA, GN, ML, MR, NE, SN, TD, TG), AP (KE, LS, MW, SD, S Z, UG), UA (AM, AZ, BY, KG, KZ, MD , RU, TJ, TM), AL, AM, AT, AU, AZ , BB, BG, BR, BY, CA, CH, CN, CZ, DE, DK, EE, ES, FI, GB, GE, HU, I L, IS, JP, KE, KG, KP, KR, KZ, LK , LR, LS, LT, LU, LV, MD, MG, MK, MN, MW, MX, NO, NZ, PL, PT, RO, R U, SD, SE, SG, SI, SK, TJ, TM, TR , TT, UA, UG, UZ, VN (72) Inventor Green, William A             90249 California, United States             State, Gardena, Faithsmith Avenue,             15626 (72) Inventor Sevaling, Kenneth W.             90611 California, United States             Province, La Abra, Brookdale Aveni             View, 1220 (72) Inventors: Hayes, Richard J.             92947 California, United States             Huntington Beach, Hunting State             Ton Village Lane, 15555, 225

Claims (1)

[Claims] 1. A container (24), on a shaft (28), rotating with respect to the container and the container; And bearing devices (54, 56, 58) for rotatably supporting the shaft at An extending shaft (50), mounted on the shaft and within the container; Spaced membrane packs where each pack has an interior for carrying the filtered fluid A stack (30) of (32) and a filtered fluid coupled inside the pack An outlet (52) for flowing air and each element is between a pair of the membrane packs. Meanwhile, the radial inner and outer gap ends (100, 110) A substantially stationary separation element within the vessel leaving a gap (40) to form A stack (34) of (36) connected to said shaft and said membrane pack A motor (26) for rotating the stack with respect to the axis, and A supply inlet (12) coupled therewith for flowing a supply fluid therethrough, the filter comprising:   The supply inlet (12) formed in the container and the radial direction of the gap; Characterized by a supply conduit (82) connected to the outer end (110) of the , The supply conduit is configured such that the supply fluid is supplied from the location of the supply conduit to the feed conduit. Flow from the gap to the location of the supply conduit. The radially outer ends of substantially all of the gaps so that A filtering device extending around the outer end of the gap for connection to a filter. 2. The separation element includes a first membrane pack (32A) and a second membrane pack. At least one central separating element (40A) between The central separation element is connected to the first membrane pack and the second membrane pack. Each facing and having a first side (160) and a second side (162) , The central separating element has a plurality of through openings (131-1) connecting its surfaces. 38)   The center separation element and the plurality of openings therein are each provided with the first separation element. Extending radially beyond the outer periphery (150) of the membrane pack and the second membrane pack To facilitate the flow of supply fluid between the supply conduit and the gap, The opening is at least one area of the first membrane pack and the second membrane pack. The filtration device of claim 1, wherein the filtration device is present at greater than 0%. 3. The rotor includes a shaft (50) having a permeate conduit (52); The filter packs each include a permeate conduit for flowing a permeate of the supply fluid. Connected to the   The shaft has axial ends (14, 14) protruding from axial ends of the container. 16) wherein the permeate conduit extends through both of the shaft ends The filtration device according to claim 1, wherein the permeate flows outside through both ends of the shaft. 4. At least some of the elements are membrane pack elements; Each of the pack elements includes a membrane sheet (105) facing a corresponding gap; Also includes a flow sheet (106) lining the membrane sheet and forming a permeate passage. The filtration device according to claim 1. 5. The gap has a radially inner portion (100), the radius of the gap being Directional inner parts are connected to each other, but radially outward along said gap 2. The flow of fluid from the container is prevented, except along an extended path. 3. The filtration device according to item 1. 6. A container (24) and a shaft (5) on axis (28) and extending into said container. 0), a spaced membrane membrane mounted on the shaft and located in the vessel. Stack (30) with each element between a pair of said membrane packs A substantially stationary separation in said vessel, leaving a gap (40) therebetween A stack (34) of elements (36) connected to and in front of said shaft A motor (26) for rotating the stack of storage packs with respect to the axis; A filter inlet comprising a supply inlet coupled to the interior of the vessel for flowing a supply fluid therethrough; And   At least one of the separation elements (36) has a small area of the separation elements. A plurality of through openings (131-138) occupying at least 10%, Having a plurality of walls (141-148) including walls on both sides of the predetermined portion, Equalized fluid pressure on both sides of the separation element A filtering device, which prevents the deflection of the separation element caused by the separation element. 7. The predetermined separation elements each have an angle of 90 ° with respect to the axis. There are four virtual sectors (164) that define a segment in each of the sectors. A plurality of openings having an area of a fan-shaped portion; Openings (131, 132) occupying at least 10% of the The filtration device of claim 6, comprising: 8. Both the predetermined separation element and the opening therein, From at least half the radius of the membrane pack to the outer periphery (150) of the membrane pack Extending further radially outwardly around the pair of gaps and the membrane pack. 7. The method of claim 6, wherein the flow of the supply fluid to and from a portion of the interior of the container at The filtration device according to claim 1. 9. The predetermined separation element includes a plurality of separation elements formed between the openings. Said element including spokes (141-148) extending mainly in the radial direction, 360 ° continuous hub (180) near the radial center of the A continuous rim (182) near the radial outer periphery to define each of said spokes. The filtering device according to claim 6, which supports. 10. The motor is located outside the membrane pack relative to an adjacent portion of the separation element. Rapidly rotate the shaft so that the peripheral speed is at least 4 meters per second Is configured to   The predetermined separation element comprises a first said membrane pack (32A) and a second Between the membrane pack (32B),   The plurality of openings in the specific separation element are mainly in a radial direction. Extending to form spokes (141-148) between the openings, wherein the spokes are Moving the spokes rapidly when the membrane pack rotates rapidly. Between the first membrane pack and the second membrane pack in the supply fluid flow 7. The filtering device of claim 6, wherein the filtering device is configured to aerodynamically center itself. 11. The opening extends along most of the radius of the predetermined separation element Four to sixteen primarily radially extending openings (131-138) And leave 4 to 16 spokes (141-148) between the openings. The filtration device according to claim 6. 12. A container (24) and a shaft (28) on the axis (28) and extending into said container. 50) mounted on the shaft and spaced apart in the container A stack (30) of membrane packs (32), each element comprising a pair of said membrane packs Substantially stationary in said container, leaving a gap (40) therebetween. Stack (34) of separated elements (36), and A motor (26) for rotating the stack of membrane packs with respect to the axis; A supply inlet (12) coupled to the interior of the vessel for flowing a supply fluid therethrough; An excess device,   A radially outer end each of the plurality of separating elements being coupled to the container; And a plurality of spokes (14) that extend primarily in the radial direction and have a radial inner end. 1-148) and a hub portion connecting the radially inner ends of the spokes to each other (180). 13. Are substantially stationary such that each of the separation elements is between a pair of membrane packs. The rotating pack surface while maintaining the stack of separated elements (36) (34). Stack (30) of membrane packs (32) having a container (24) in a container (24). Rotating about an axis (28), wherein each element is an element surface (113), wherein the pack and the element are in contact with the surface of the rotating pack. A first turn of the membrane pack, leaving a gap (40) between the first and second membrane packs. A first gear between the transfer pack surface and a first element surface of the first said element; And a feed fluid (90) to be separated into a permeate and a concentrate. A rotary filtration device comprising feeding to the vessel for entry into the gap A method for operating the device,   An inward position within the first gap and adjacent to a location on the first element The feed fluid is at least partially radially inward along the path (102). Flushing, wherein the first gear is adjacent to the first element. Substantially all of the feed fluid in the tap is radially inward instead of radially outward Flows with the components of   Transferring some of the permeate from the feed fluid to and into the first membrane pack Flowing into the permeate conduit (52) from the first gap, Along the outer path (94) adjacent to the rotating pack surface of the first membrane pack. Flowing at least partially radially outward of some of the feed fluid. The supply fluid substantially adjacent to the rotating pack surface and within the first gap; All flow in the radially outward component instead of the radially inward one, A path and at least some of the outer path substantially above the first element In the same place,   Radially along the inner path and the outer path in the first gap A part of the supply fluid flowing inward and radially outward is divided into a plurality of gaps. To a feed conduit (82) connecting them to each other. How to operate the device. 14． The supply conduit (82) is in the container and is at least partially axially Extending radially outwardly from the stack of membrane packs,   Flowing the feed fluid at least partially axially along the feed conduit From the supply conduit to each of the plurality of gaps, and Flowing a supply fluid from each of the gaps to the supply conduit. 14. The method according to claim 13. 15. Starting a process to clean the stack of membrane packs; ,   Before starting the process for cleaning the membrane packs of the stack A gap between each of the rotating pack surfaces and an adjacent one of the element surfaces. On the rotating pack surface only to a thickness of less than one tenth of the Accumulating particles of the feed fluid.