MXPA99001941A - Modular filtration system - Google Patents

Abstract

The weight of a fluid is used to drive a plurality of semi-permeable membranes or other filter material to produce a permeate, and in at least some level of the apparatus more than 30%of the permeate produced is collected within a single casing (32). In other aspects, the filter material is at least partially contained within series production modules (40), which may contain transport zones for transporting feed or flushing fluid. In other aspects the ends of adjacent production modules may be designated to mate with one another using a slip fit, and the production modules may be maintained in matting relationship through connections to supporting cables or rods (23). In other aspects of the inventive subject matter a submerged pump (53) may be used to raise permeate towards the surface, and the pump may advantageously operate at least partially using centrifugal force and/or air lift principles. In still other aspects feed fluid can be provided from salty or brackish water source such as an ocean or bay using pipes having removable inlet plugs which resist clogging, and it is contemplated that such pipes can be laid using an underwater sled which digs a trench while concurrently laying the pipe.

Description

I-ODUIA FILTRATION SYSTEM Field of the Invention The present invention relates generally to fluid filtration, especially including filtration of water.

Background of the Invention Despite numerous advances over the years, there is still a continuing need for water purification. Many areas of the world have insufficient fresh water to drink or for agricultural purposes, and in other areas where there are abundant supplies of fresh water, water is frequently contaminated with chemical or biological contaminants, metal ions and the like. There is also a continuing need for commercial purification of other fluids such as industrial chemicals and food juices. The U.S. patent No. 4,759,850, for example, describes the use of reverse osmosis to remove alcohols from hydrocarbons in the additional presence of ethers, and U.S. Pat. No. Ref.029571 4,959,237 describes the use of reverse osmosis for orange juice. Many of these needs have been solved by filtration, and in pcular by reverse osmosis, in which the constituents are separated under pressure using a semipermeable membrane. When used herein, the term "membrane" refers to a functional filter unit, and may include one or more semipermeable layers. Depending on the fineness of the membrane used, reverse osmosis can remove pcles that vary in size from macromolecular to microscopic, and modern reverse osmosis units are able to remove pcles, bacteria, spores, viruses and even ions such as Cl "or Ca ++ There are several problems associated with large scale reverse osmosis (RO), including excessive fouling of the membranes and the high costs associated with the production of the pressure required through the membranes." These two problems are interrelated because most or all of the known RO units require cleaning by applying a jet of liquid to the membranes during operation with a relatively large amount of the feed liquid in relation to the amount of the substance lost produced. of the rejection of the liquid for washing with the jet with respect to the recovery of the substance p ermed, in the desalination of seawater, for example, is approximately 3: 2. Because only some of the seawater that is used is recovered as purified water, the energy used for the remaining water is wasted, creating an inherent inefficiency. There have been numerous attempts over the years to improve the efficiency and effectiveness in terms of the concomitant cost of RO units. The U.S. patent No. 5,229,005 to Fok et al, for example, describes lowering a container from the side of a boat entering the ocean. The vessel is equipped with an RO membrane on one of its surfaces, and at a depth of approximately 700 meters, the pressure at the depth is sufficient to force fresh water through the membrane and into the vessel. When the container is thus filled with fresh water, it is again raised to the ship and emptied. To increase the efficiency of the operation, the inventor suggests alternately lowering and emptying two such containers. Although the claimed method may be functional, the non-continuous nature of the process makes it largely unsuitable to supply fresh water on a commercial scale.

Another attempt to improve the cost effectiveness of RO units is described in U.S. Pat. No. 4,512,886 to Hicks et al. There, an RO module is placed in the ocean at a depth at which the pressure of the environment is insufficient to operate the membrane, but at such a depth the pressure combined with an additional pressure provided by a pump is sufficient to operate the membrane . The pressurized water is therefore pumped through the RO module using the energy of the upper waves, with the fresh water that arrives or comes on one end of the module, and the brine that is eliminated at the other end. Unfortunately, the mechanism is limited to places that have significant swell action, and in any case it is relatively expensive to install and operate. Yet another attempt to improve the cost effectiveness of RO units is described in U.S. Pat. No. 3,456,802 to Colé et al. In this patent, several RO cells are submerged to a sufficient depth in the ocean, and the pre-filtered salt water is filtered on the surface and fed down the cells through a pipeline. The output of fresh water from the cells is then pumped back to the surface, while the wash or flood water is returned to the ocean. For this mechanism, Colé et al, claim that the useful life of the membrane is increased by prefiltering the salt water applied against the membranes, and increasing the speed of flooding or cleaning with a jet of liquid. What could not be overcome, however, was the requirement of proximity to a deep expanse of water outlet, and the difficulty of replacing the RO cells. The requirement of proximity to a deep salt water extension in desalination operations is addressed in U.S. Pat. No. 4,125,463 to Chenoweth, which is incorporated herein by reference herein in its entirety. In the Chenoweth patent, numerous semi-permeable membrane assemblies are placed inside a well or other underground cavity. The salt water flows down to the membranes from above, and the hydrostatic pressure of the salt water drives the permeated substance through the membranes. The permeated substance, which in this case is purified water, is then pumped out of the system through a riser or vertical pipe. The main advantage contemplated by Chenowest is that energy consumption is largely restricted to the pumping of purified water.

Despite the reduced energy consumptions contemplated by Chenoweth, the design is not practical. Among other things, the Chenoweth design teaches in elevator or central vertical tube surrounded at many different depths by groups of five satellite RO units. Each of the satellite units has its own collector, and the various collectors of each group flow together towards a manifold in the elevator or central vertical pipe. Such a design is inherently inefficient. The grouping of satellite RO units adds unnecessary complexity and cost, and the presence of multiple satellite envelopes or jacketing at the same level wastes a valuable channel volume. There is still a need for an apparatus and methods to effectively purify large amounts of fluid using pressurized filtration in a cost-effective manner.

Brief Description of the Invention In the present invention an apparatus and methods are provided in which the upper pressure developed by the weight of a fluid is used to drive or drive a plurality of filters to produce a permeated substance, and to at least some level (ie to the same depth) within the apparatus, at least 30% of the permeated substance produced is collected within a single filter casing or jacket. The subject matter of the invention can reduce or eliminate by this grouping in systems based on channels and other filtration systems, and thus provides improved efficiency and cost effectiveness. In the preferred embodiments, substantially all of the filter material at a given depth is wound around one or more collectors of the permeated substance into a single filter liner. In even more preferred embodiments, the filters and the lengths of the collector tube (s) form the internal cores of a series of production modules. In the especially preferred embodiments, each of the production modules further includes a transport zone for transporting the brine and a transport zone for transporting the permeate. In other aspects the ends of the adjacent production modules can be designed to correspond to each other using a sliding fit seal, and the production modules can be maintained in casing relationships through the connections to support the cables or rods. In still other aspects of the subject matter of the invention, a submerged pump can be used to raise the permeate to the surface. In the preferred embodiments having this characteristic, the pump can operate at least using pneumatic and / or centrifugal rising principles, and where a pneumatic rise principle is used, an energy recovery system can be used to recover the energy of the pump. fluid and gas rising. It is also contemplated to employ a gas produced by means of electrolysis to aid pumping. Still other aspects of the feed fluid can be provided from a salt or brackish water source such as an ocean or bay using pipes having re-usable inlet adapters which resist plugging. It is also contemplated that such pipes can be deposited using an underwater sled which digs a trench while at the same time depositing the pipeline.

Brief Description of the Drawings Various objects, features, aspects and advantages of the present invention will become more apparent from the following detailed description of the preferred embodiments, in conjunction with the appended drawings, wherein like reference numerals represent like components. Fiqura 1 is a schematic view of a reverse osmosis system. Figure 2 is a schematic view of a module of production. Figure 3 is a schematic perspective view of a production module. Figure 4 is a vertical cross-sectional view of the production module of Figure 3 at 4-4. Figure 5 is a vertical cross section of the production module of Figure 3 at 5-5. Figure 6 is a perspective drawing of a transition assembly that is installed or removed. Figure 7 is a perspective drawing of a portable lifting tool. Figure 8A is a schematic view of a wrapped or liner filter sub-assembly.

Figure 8B is a schematic view of an unswrapped filter sub-assembly or liner. Figure 8C is a more detailed schematic view of a portion of the non-enveloped filter sub-assembly or liner of Figure 8B. Figure 8D is a schematic view of an alternative filter sub-assembly in which the filter material is shown in a bent or folded configuration. Figure 8E is a schematic view of another alternative filter sub-assembly.

Detailed description of the invention In Figure 1 a filtration system 10 generally comprises a floating winch 11, a plurality of transition modules 60, a pumping module 50, a plurality of production modules 40, and cables 23 which support the various modules. The floating winch 11 and several modules 60, 50, 40 all cooperate to provide a flow path of the feed liquid 18, a flow path of the permeate substances 18A and a flow path for the wash liquid with a jet 19.

The various modules of the system 10 may be contained in a well or other channel (not shown), or they may be located in an open ocean or other extension of water (not shown). In the case of a well or other channel, one of the flow paths 18, 18A or 19 can advantageously be formed as an annular space between the outer shells or casings of the modules 60, 50, 40 and the coating 20 of the channel. Where the system 10 is positioned within an ocean or other open expanse of liquid, the flow paths of the feed liquid and the flood or flush liquid, 18 and 19, respectively, may comprise the open spread of the liquid . When used herein, the term "channel" is generically used to mean a space that has a relatively narrow and relatively deep portion which may contain a fluid. Therefore, an ocean, bay, lake or other large expanse of water can not be considered as a channel as the term is used here because such extensions are wide relative to their depth. On the other hand, a well of water or oil, or an underwater camera connected by means of a passageway could all be considered as channels as the term is used here. It is desirable that the channel have a usable internal diameter of at least 14.24 cm (6 inches), although channels having smaller diameters can also be used. The coating of the channel is not particularly important, and suitable channels may have steel linings, cast iron, concrete or other linings, or they may not have any coating at all. In many cases a channel used in accordance with the present invention may be located near the ocean or other salty or brackish water extension to provide a convenient source of water. In such cases the channel may descend from a point in the extension of the water or from a point on the ground. In other cases you can use an appropriate channel which is many kilometers from a water source. The appropriate channels can still be tilted instead of vertically oriented. In summary, the apparatus and methods as described herein can be used in conjunction with many different types of channels, without taking into account their original purpose, form, orientation, and location. In the floating winch 11 a feed liquid, which may comprise, for example, salt water or brine, is fed into the system 10 by means of the supply of the feed liquid 12, while the waste liquid is expelled in the discharge of the flood or wash liquid 14, and the purified liquid (permeated substance) is expelled in the discharge of the permeate 13. The supply of the feed liquid 12, the discharge of the permeate 13 and the discharge of the flood liquid 14 can be welded or otherwise secured to the floating winch 11. In preferred embodiments particularly, the system 10 can be pressurized to approximately 3 bars by the feed liquid pump 56. This helps to overcome friction losses in the flow path of the feed liquid 18, the pressure losses through the production assemblies 40, and friction losses in the flow path of the flood liquid 19. A prefiltration system 57 may optionally be employed where appropriate, depending on the concentration of the particulate substances in the feed liquid. A receiving tank 58 can also be used to receive the permeated substance. The transition modules 60 are primarily designed to provide conduits between the floating winch 11 and the pumping module 50. The transition modules 60 can therefore be very simple in design, such as a pipe within a pipe (not shown). ), or one or more collector tubes placed in a collateral configuration (not shown). The pumping module 50 generally comprises a centrifugal pump 53 or another pump which elevates the permeated substance from the production modules 40 to the floating winch 11. The pump 53 is most likely electrically operated, and the electrical energy can be brought to the pump using a power cable (not shown). Alternative pumps may operate using some other force, such as compressed air, and it is particularly contemplated that pump 53 may comprise a pneumatic lift pump or a compound pump which utilizes a pneumatic lift principle. In such circumstances the gas used could be compressed on the surface and transported to the pump using a high pressure gas line, or at least some of the gas could be produced at or near the pump by means of electrolysis. In other embodiments, the system 10 may include multiple pumping modules (not shown), or a single pumping module may contain more than one pump. It is advantageous to provide a rising and falling pumping means 53 without dismantling the transition modules 60, and this can be effected using installation cables 51 of the pump. It is contemplated that the pump 53 may be used to reduce the positive net suction to about one bar, and to discharge the permeated substances into the flow path of the permeated substance 18A between 60 and 70 bar. The actual discharge pressure is at least partially a function of the depth below the surface to which the pump 53 is mounted and the salinity of the feed liquid. The production modules 40 generally comprise an input sub-assembly 70 and a plurality of adjacent filtering sub-assemblies 30. The intake sub-assembly 70 directs the supply liquid from the flow path of the supply liquid 18 to the higher or more filtration sub-assembly. lower 30, and direct the flood or flushing liquid away from the filters 35 contained within the filtration sub-assemblies 30. As described below in greater detail with respect to Figure 2, the filtration sub-assembly 30 contains one or more filters 35 which separate the feed liquid in the permeate and the flood or flushing liquid.

It is contemplated that the production modules can be placed at depths of at least about 50 meters. Such depth is sufficient to effect reverse osmosis on brackish water using commonly available membranes, and it is expected that when the membrane technology improves, the production modules will work well at depths of less than 50 meters. On the other hand, it is contemplated that the systems will use filters at a wide range of depths, including the depths of at least 100 meters, at least 250 meters, at least 350 meters, at least 500 meters, at least 750 meters, and at least 1000 meters. The cables 23 are used to hold or hold together several modules 60, 50, 40 together, and to support their weight. As described in more detail below with respect to Figure 5, the cables 23 can be replaced with bars (not shown), rods (not shown), belts (not shown), and other supports, and alternatively can be eliminated together using other means of connection and support between the adjacent modules. Modules 60, 50 and 40 can be constructed in virtually any workable shapes and sizes, using virtually any suitable materials, and not all modules need to have the same structural or compositional characteristics. For reasons of convenience and cost effectiveness, it is contemplated that the transition modules 60, the pumping assembly of the permeated substances 50, and the production modules 40, will be substantially tubular, and will be constructed primarily from suitable materials. In particular, construction materials such as PVC, epoxy glass fiber, stainless steel or other steels can be used. Still other construction materials may include new compounds or materials not yet developed. In operation, the production modules 40 will generally be joined or otherwise juxtaposed end to end with other production modules 40 to form a chain. One or more pumping modules 50 could be placed on top of the uppermost production module, and the transition modules 60 could be added above the pumping module (s) to reach the floating winch 11. mounts could be lowered to an open area or channel to the required depth using an apparatus such as that shown in Figures 6 or 7.

The various modules are preferably coupled using sliding fit couplers. In the alternative embodiments, however, two or more modules may be coupled by other means, including threaded connections, clamps, bolts, and glued. It is also contemplated that the systems according to the subject matter of the invention may be associated with some kind of support installation, which may include one or more constructions, pumping houses and so on. Although not explicitly shown, it is anticipated that the feed fluid may be pre-filtered, and such pre-filtration may occur at any point upstream of the supply of feed liquid 12 passing to the production assemblies 40. The ability to pre-filter the salt water extracted from an extension of water such as a bay or ocean may be relatively important in terms of the long-term protection of the filter material, and may make devices and methods superior in accordance with the present objective with respect to those of placing only the filters in the open ocean, and resting either on the natural water currents or the pumping water that passes through the filters to achieve a proper washing or flooding.

Turning to Figure 2, a production module 40 generally comprises one or more filter sub-assemblies 30 and a single transition sub-assembly 70. Each filter sub-assembly 30 comprises an external shell 31, an annular space 19A, and one or more filter sub-assemblies 44. As best shown in Figures 8A-8E, each filter sub-assembly 44 may advantageously comprise one or more filter liners 32, each of which can accommodate a plurality of filters. filter sheets 35 and spacers 41 coupled to a collection tube 33. As described further below, Figure 2 shows a plurality of openings 74 of the entry holes contained in the input subassembly 70, which communicate the fluid from the path of flow of the feed liquid 18 through the rungs 77, and into the feed area of the filter 78. Figure 2 also details a possible coupling 22 between the wire 23 and the production module 40. The coupling can also be carried at any point or points along the production modules 40, but it is preferred that such coupling will be carried out near the top and near the inf of the production assemblies 40. There are many alternative configurations of the production modules, which, although not shown in the present drawings, are consistent with the inventive concepts herein. For example, it is not necessary for the fluid transport annulus in the production modules 40 to be annular, and it is not yet necessary for the production modules 40 to include a fluid transport zone. As described below, the feed liquid can be transported in a space between the production modules and the channel cover, and it could also be possible to transport the permeate liquid or feed liquid to a separate pipe or external compartment to the modules of production. Similarly, in the alternative embodiments, the filter sheets 35, the spacers 41 and the collector tube (s) may be placed differently from that shown here. In Figure 3 a preferred arrangement includes three filter sub-assemblies 30 grouped by the single transition sub-assemblies 70. However, it should be appreciated that a larger or smaller number of filtering sub-assemblies 30 could be located between the transition sub-assemblies 70, and it is particularly contemplated that a filtration system used in salt water desalination could have, five series of filter sub-assemblies 30 mounted, located between the transition sub-assemblies 70, each filtering sub-assembly 30 being approximately six meters long. The number five is contemplated to be particularly advantageous because it is thought to properly balance the flow velocity (flood) against the pressure drop and the recovery speed. In Figures 4 and 5 arrows are used to indicate the possible flow directions of the feed liquid. In the particular embodiment shown, the feed liquid flows down along the flow path 18, through the inlet openings 74, along the rungs 77, and towards the filter feed area 78. The feed liquid then flows down through the spacers 41 (see Figure 8C), where it is divided by the filter material 45 into separate streams of flood or wash liquids and permeate substances. The permeate liquids then pass through the collecting orifices 34 and into the collecting tube 33, from which they flow upwards towards the pump for the permeated liquids 53. At the same time, the flood or cleaning liquid with a continuous jet flowing down through the spacers 41 of one or more filter sub-frames 44, until it reaches the collection space 79 located within the next lower transition sub-assembly 70. The flood or flushing liquid then leaves the sub-assembly of transition 70 and passes upwards through successive higher production modules 40, the pumping module 50 (not shown), and the transition modules 60 (not shown) toward the floating winch (not shown). In Figure 6 a top transition module 60U is being coupled or uncoupled from a lower transition module 60L. In this particular embodiment, each transition module 60U, 60L has an external pipe 61 and an internal pipe 62. The external pipes 61 are coupled through the sliding fit coupling 61A, and the internal pipes 62 are coupled through the coupling of the coupling. Sliding adjustment 62A. In addition, the annular seals 61B and 62B are used to seal the pipes 61 and 62 respectively. Still further, the optional guide rims or rungs (not shown) can advantageously be deployed in the various annular spaces, such as between the pipes 61 and 62, and between the pipe 61 and the coating of the channel 20. Of course, as shown in FIG. noted above, the couplings shown in Figure 6 are only exemplary, and other types of couplings and connection strategies are contemplated as well. Passing the wiring, the cable 23 comprises the terminal of the upper cable 27, the lifting point 28, the resting point 29 and the lower cable terminal 26. The connecting bolts 27A are used to fix or secure the coupling between the cables adjacent 23, and the cable clamps 25 are used to couple the cables 23 to the modules 60. It should be appreciated that although each cable is only as long as the module 60 in this particular embodiment, each cable may be longer or shorter that a corresponding module, and a single cable can extend along the entire length of the system 10. It should also be appreciated that the clamps 25 of the cable shown, are different in design from the clamps 22 of the cable of Figures 2 and 3, and that other types of means of arresting or securing the cable are also contemplated. The lifting assembly 80 can also be used to mount or dismount the system 10. There are many possible configurations here, including the assembly 80 shown, which comprises the telescopic support 82 and the rams 81. Figure 7 shows a portable mechanical lifting assembly 90 which includes a telescopic support 92 and the rams 91. Also shown is a harness or lifting equipment 95, which is used to bolt the terminal 27 of the upper cable and raise or lower any of the modules 60, 50 or 40. The lifting assembly 90 can be controlled by any convenient controller, including the transportable control panel 94. In the preferred embodiments of Figures 8A and 8B, two or more discrete filters are folded and glued in the filter sheets 35, and spirally wound. around the collector tube 33, in the company of the interspace 41 spacers. This design produced high pressure sides and low pressure sides of the filter sheets 35. It should be appreciated that it is not necessary to have more than one filter sheet 35 placed around the collector tube 33, and it is not necessary for the arrangement, comprising the liner or envelope. In alternative embodiments, for example, it is contemplated that the filter (s) of the sheet (s) could be partially rolled and / or partially bent around the manifold 33.

Additional details of the preferred embodiments of the filter 35 are shown in Figure 8C. Here, each of the filter sheets 35 comprises a layer of filter material 45 on each side of a carrier material 42 for the permeate liquids. The carrier material 42 for the permeate liquids is sealed in the seal 43 and drains into the collecting holes 34 provided in the manifold tubes 33. As noted above, a spacer 41 is placed between the overlying filter sheets 35. The liquid feed that does not pass thr the filter sheets 35 could continue to flood the high-pressure side of the sheets 35, and could eventually be taken out of the system by way of the flood flow path 19. The filter material 45 contemplated herein includes, but it is not limited to the membranes used in reverse osmosis processes. Therefore, the material object of the invention can use materials designed to filter macroparticles (100 to 1000 micrometers), microparticles (1.0 to 100 micrometers), macromolecular particles (0.1 to 1.0 micrometers), molecular particles (0.001 to 0.1 micrometers). or ionic particles (less than 0.001 to 0.001 micrometers). Future filter designs can increase the filtration interval even further to include even smaller particles, and perhaps even molecular lysis, such as hydrogen that separates from oxygen as in hydrolysis. In this way, the contemplated processes could cover the full filtration spectrum for liquids. The filtration spectrum identified above could include particle filtration, and continue thr Microfiltration, Ultrafiltration, Nanofiltration and Hyperfiltration (Reverse Osmosis). It is contemplated that a single external shell 31 could contain the multiple filter liners 32. In such an embodiment multiple manifolds 33 may be employed while still maintaining efficient use of space within the jacket or liner 32, and such an arrangement satisfies the limitation of that at least some level within the apparatus of at least 30% of the produced permeate liquid is collected within the sub-assemblies 30 of a single filter at any given level. In other preferred embodiments, 40%, 60% and up to substantially all of the permeate liquid produced is collected from within the single filter subassemblies suspended at any given depth. In much less preferred embodiments it would also be possible to provide multiple filter sub-assemblies 30 at a given depth. But for purposes of this application the 30% limitation has been chosen to distinguish and provide a significant advantage over Chenoweth. In Chenoweth there are always five different membrane assemblies in each production level. This selection is obviously made to efficiently accommodate conventional membrane assembly groups, at a given depth, within a round wellbore. Alth Chenoweth does not teach or suggest improvement, it may also be possible to provide only three different membrane assemblies at each depth of production. Such Clustering could produce approximately one third of the permeate liquid at a given depth within each of the three filter shells or liners, and for this reason the 30% limitation has been chosen. Turning to the still alternative modalities, it is contemplated that a collecting tube 33A of the permeate liquid could be placed in another position different from the central position (as in Figures 8D and 8E), or that the collector could be placed completely outside the filtering sub-assembly. . For example, one or more manifolds (not shown) could be placed within the production assembly 40, and the permeate liquid could flow from the manifold (s) to an external section comprising a new annulus (not shown). Again the critical limitation is that at least at some level within the apparatus greater than 30% of the permeate liquid produced at a given depth, is collected within the single filter sub-assembly 30. Of course, the invention is not limited to the modalities shown and described specifically. In the alternative modalities, for example, any of the liquid flows could operate in reverse fashion to that described here. Alternatively, the various fluid flow paths could be exchanged. Accordingly, in Figure 2 the fluid flood could exit the doors 74 instead of the feed fluid being introduced to the doors or openings 74. In other embodiments, the system and methods described herein could be used to purify the foods such as orange juice, or to separate several industrial chemicals. Accordingly, although the specified embodiments and applications have been shown and described, it may be apparent to those skilled in the art that many modifications are possible without departing from the inventive concepts herein. The invention, therefore, will not be restricted, except in the spirit of the appended claims.

It is noted that in relation to this date the best method known by the applicant to carry out the aforementioned invention, is that which is clear from the present description of the invention.

Having described the invention as above, property is claimed as contained in the following

Claims (19)

1. A method of purifying a fluid, characterized in that it comprises: placing the fluid in a passageway; providing a plurality of filter liners or envelopes in the passageway, each having a filter and a manifold operatively coupled to employ a hydrostatic head pressure as a substantial force in driving at least a portion of the fluid through the filter to produce a permeated liquid; providing a common permeate fluid conduit which conducts the permeate fluid produced within at least two of the liners or wraps of the filter, and around which the filters are circumferentially distributed; and placing the liners or wraps around the permeate fluid conduit such that at least 30% of the permeate fluid produced at a given depth is produced within only one of the liners or wraps of the filter.

2. The method according to claim 1, characterized in that the step of disposing of the fluid comprises disposing of the fluid in a perforated channel in an area of the ground.

3. The method according to claim 2, characterized in that the channel has a depth of at least 50 meters.

4. The method according to claim 2, characterized in that the channel has a depth of at least 250 meters.

5. The method according to claim 1, characterized in that the step of providing a filter comprises providing a semipermeable membrane.

6. The method according to claim 1, characterized in that at least 40% of the permeate liquid produced at said depth is collected within only one of the liners or wraps of the filter.

7. The method according to claim 1, characterized in that at least 60% of the permeate liquid produced at said depth is produced within only one of the liners or wraps of the filter.

8. The method according to claim 1, characterized in that substantially all of the filter at a given depth is placed within only one of the liners or wraps of the filter.

9. The method according to claim 1, characterized in that it further comprises arranging multiple filters in at least two stacked production modules having a first transport zone for transporting the permeate liquid, a second transport zone for transporting a supply portion of the fluid , and a third transportation zone for transporting a portion of fluid flooding.

10. The method according to claim 9, characterized in that it further comprises providing at least two production modules with a sliding fit connection.

11. The method according to claim 9, characterized in that it also comprises keeping the production modules in a relative or matching relationship through the connections to support the cables or rods.

12. The method according to claim 1, characterized in that it also comprises: using a submerged pump to raise the permeate liquid to the surface or to the ground level.

13. The method according to claim 12, characterized in that the pump operates at least partially using a pneumatic lifting principle.

14. The method according to claim 13, characterized in that it also comprises electrolyzing the fluid to produce a gas.

15. The method according to claim 1, characterized in that it also comprises extracting the fluid from a water source using the pipes having removable inlet plugs or adapters.

16. The method according to claim 14, characterized in that it also comprises depositing the pipes using an underwater sled which digs a trench while depositing the pipe at the same time.

17. The method according to claim 1, characterized in that: the step of disposing of the fluid comprises discarding the fluid in a channel having a depth of at least 250 meters; wherein the step of providing a filter comprises providing a semipermeable membrane, and at least 40% of the permeate liquid produced at said depth is collected within only one of the liners or shells.

18. The method according to claim 1, characterized in that: the step of disposing of the fluid comprises disposing the fluid in a channel having a depth of at least 250 meters; and the step of providing a filter comprises providing a semipermeable membrane; and further comprising placing multiple filters in at least two stacked production modules.

19. The method according to claim 1, characterized in that the step of disposing the fluid comprises disposing the fluid in a channel having a depth of at least 50 meters and the step of providing a filter comprises providing a semipermeable membrane, and further comprising placing multiple filters in at least two stacked production modules, and maintain the production modules in casante or corresponding relationship through the connections to support the cables or rods. SUMMARY OF THE INVENTION The present invention uses the weight of a fluid to drive or drive a plurality of semipermeable membranes or other filtering material to produce a permeate fluid, and at least some level of the apparatus greater than 30% of the produced permeate liquid is collected within a liner or wrapper (32). In other aspects, the filter material is at least partially contained within the series production modules (40), which may contain transport zones for transporting the feed or flood fluid. In other aspects the ends of the adjacent production modules can be designed to correspond to each other using a slip adapter and the production modules can be maintained in a matching or corresponding relationship through the connections to support the cables or rods ( 2. 3) . In other aspects of the subject matter of the invention, a submerged pump (53) can be used to raise the permeate liquid to the surface, and the pump can advantageously operate at least partially using the centrifugal force and / or pneumatic lifting principles. In still other aspects the feed fluid can be provided from a source of salty or brackish water such as from an ocean or a bay using pipes having adapters or inlet plugs which resist plugging, and it is contemplated that pipes can be deposited using an underwater sled which digs a trench while at the same time depositing the pipeline.