TW508265B - Multi-Stage filtration and softening module and reduced scaling operation - Google Patents

Abstract

A filtration module has a plurality of hollow fibre nanofiltration or reverse osmosis membranes suspended between a pair of opposed headers. The lumens of the membranes are the retentate or feed side. The membranes are arranged in groups, such as sectors of a cylinder, and form preceding or succeeding stage. A permeate collection plenum is in direct fluid communication with each stage. The stages are connected by caps typically having dividers located at the ends of the module. The module is used to filter water and, when optionally fitted with hollow fibre membranes adapted to selectively reject hardness causing salts, is used to remove hardness. Methods of cleaning using acidic solutions or gaseous carbon dioxide are discussed. Cleaning methods include adding acid to the feed water continuously or periodically during permeation, flushing the module with an acidic solution while not permeating and holding an acidic solution or gaseous carbon dioxide in the module for a period of time while not permeating followed by flushing. A filtration system is also disclosed.

Description

508265 V. Description of the invention (i) Field of the invention The present invention relates to a multi-stage nanofiltration or reverse osmosis membrane module, a method for filtering water or removing hardness using such a module, a method for cleaning or maintaining the permeability of the module, and Particularly suitable for small systems in private homes and small commercial buildings. BACKGROUND OF THE INVENTION Hollow fiber semi-permeable membranes can be used to filter fluids containing large amounts of solids. Separator membranes in the range of nanofiltration and reverse osmosis can also be used to separate plutonium. For example, U.S. Patent No. 5,152,901 describes a nanofiltration membrane material that can filter out suspended solids and large organic molecules. Generally, it rejects calcium rhenium and allows sodium rhenium to pass through. U.S. Patent Nos. 4,812,270 and 5,658,460 also describe membranes that can be used to repel tritium. Similar membranes such as Stork Friesland's NR 015-500 are commercially available. The diaphragm is used in the form of hollow fibers and operates in an outflow mode. Hollow fibers are suspended between a pair of opposing tube sheets or heads. The head maintains the internal cavity of the septum separated from its outer surface. Therefore, pressurized feed water can be supplied to the inner cavity of one end of the diaphragm, while permeate is collected when it leaves the outer surface of the diaphragm, and concentrated or retentate is withdrawn from the inner cavity at the other end of the diaphragm. However, the various characteristics of hollow fiber membranes are difficult to use in such an outflow mode. For example, a hollow fiber with a small inner diameter causes significant pressure, while going to the exit end of a long hollow fiber will reduce the flow. U.S. Patent No. 5,013,437 describes an attempt to reduce the problems of pressure and throughput in filaments. In one specific example of the patent, the core fiber filtering module flowing out from the inside is divided into two stages. The stagnation of the first stage becomes

Page 7 V. Description of the invention (2) The first 6 feeds. The surface area ratio of the first pair of the second stage is preferably about 1.5: 2 to 2.25: 1. This helps to become the first stage retentate of the second stage feed. The increased pressure section has closer equal pressure,], and direction. The second stage is arranged concentrically, and the permeate in the second stage must be the outer side of the fiber Flow and reach the exit. The reasonable density of the hollow fiber membrane is used to filter the liquid, and the drop loss in the permeate stream will be mild. Therefore, the transmembrane pressure difference across the second stage diaphragm decreases. It is also difficult to fit the fibers into an annular ring, as required in the patented membrane pack.

Similar principles are used in large systems where spirally wound diaphragms are used. For large f, the film die stage is configured in stages. The modules in each subsequent stage are better than the leading stage ptl / 1, bar # 夕 ’and the retentate in the leading stage becomes the feed for the subsequent stage. This kind of ^ ^ is complicated and is not suitable for home or small business systems. Saki and your manufacturers of micro-transition or reverse osmosis membrane filtration systems typically use strict jj ratio & i loop-to-feed Θ ^ filtration, mold stage to deal with the above problems' retain the recyclate in the system , = Γ 'to increase feed water speed and transmembrane pressure. In this case, the minimum velocity of the retentate / retentate is between about 3-10 ft / s. This results in a fast-removing diaphragm and operates at extremely low per-pass recovery rates. You need to be able to sign the second person's scale. Either you need to clean it often or you need to replace the diaphragm. Therefore, costs and pressures are also high. The other of semi-permeable membrane _

When the water is softened, the nature is that after a period of time, especially in the diaphragm system, the carbonic acid is the scale of the tritium carbonate, which causes the cell to scale. In the strike system or in the feed water i 1 you can use a resin exchange bed to soften the feed water partly,… anti-fouling agent to handle. This technology is generally used in small

508265 V. Description of the invention (3) In Tongtong, especially in residential houses, the implementation is too complicated. SUMMARY OF THE INVENTION The object of the present invention is to provide a membrane filter module. Another object of the present invention is to use the scale method, especially for water softening to provide a small filtration or water softening system. Features, steps, or both do not contain all the necessary special features of the present invention 'or with other parts of the case. In all aspects of the office, the outer surface of the centrifugal fibrous microfiltration or reverse osmosis membrane of the present invention is sealed at the head, and the conventional technology is introduced. A secondary object of the present invention is, in particular, those which can be used for small filtration or water softening to provide cleaning or reduce the formation of diaphragm modules. Another object of the present invention is. These purposes can be solved by a combination of patent applications. The following comprehensive midpoint 'is explained in the sub-feature combination of the following features. A filter module is provided with a composite hollow membrane 'suspended between a pair of opposed heads. Its inner cavity opens on the peripheral surface of the head

The subsequent fluid phase at the end of the step cavity—the end and the mouth, and the outermost area, is the area immediately adjacent to @ 即 士 在 ί • In the module, the hollow fiber membrane is grouped into a plurality of leading or Λ both segments and leading and Successor), the inner and outer ends of the hollow fiber membrane are open. Flow occurs between the phases, and the surface is connected to the-end of the first phase, and the remaining 1 ^ after the first phase is connected in series with the fluid connection between the first ends of the leading phases and the subsequent phases. The second: end of module 2 is in fluid communication. The permeate is in fluid communication. The surface of the separator in each leading stage; the successor P is between 2 and 5 times the surface area of the diaphragm, and decreases from the first stage to the last stage. ^ & Table

508265 V. Description of the invention (4) To form the connection between the stages, the first cap covers the peripheral surface of one head and the second cap covers the peripheral surface of the other head. The permeate chamber contains the space between the proximal end of the head and the shell. The separator plate in one or two caps collects the diaphragm group into the stage, leaving the fluid connection between the second end of each leading stage and the first end of each subsequent stage opened. Typically located at the module inlet and outlet of the module retentate, they are in fluid communication with the first end of the first stage and the second end of the final stage, respectively. Therefore, the feed water enters the wide first end of the first stage, and the impermeable portion leaves at the second end of the first stage. Thus, the second end cap guides the feed / retentate to the first end of the second stage. -Impervious water reaches the first cap in the second stage. In a two-stage installation, impermeable water leaves the module. In a multi-stage module, the first cap redirects the feed / retentate to the first end of another stage, and the impervious water flows to the second cap, and so on, until it reaches the end So far the second end of the stage. The configuration of the stages is such that the periphery of each module is adjacent, and the flow between the stages is generally parallel to the periphery of the module. For example, a stage may constitute a sector of a cylinder. In smaller modules with a diameter of about 3 inches or less on the Model _, the diaphragm can be divided into stages using the spokes in each header. In larger modules, the diaphragm sets can be installed separately or simultaneously — in pairs of opposing collars that can be shaped like sectors. Once installed in the pair of collars, the diaphragm can be coated. The pair of collars are then glued together to form a pair of heads. If the collars are formed of segments, the heads are cylindrical. Paired collars are easier to work with than large cylindrical heads, especially for drying in the diaphragm coating process. The divider that separates the stages can be equivalent to a collar edge or a spacer inserted into the collar. ^

Page 10 508265 V. Description of the invention (5) In a specific example, the partition plate between the stages is equipped with a valve configured so that when the feed water flows into the module in the reverse direction, it can enter through the retentate outlet of the module. The baffle packs the baffle assembly into a second leading and a second succeeding stage having a first end and a second end. The divider plate opens a fluid connection between the second end of each second leading stage and the first end of each second subsequent stage, generally parallel to the periphery of the module. When the diaphragms are reassembled, the surface area of the diaphragm in each of the second leading stages is between 1 and 2.5 times the surface area of the diaphragm in the second subsequent stage, and the surface area of the stages :: is decreasing from the first stage to the last stage. This is achieved by using a one-way valve. The opening direction is to make the diaphragms group and regroup, using the liquid effect flowing through the mold-group, that is, the pressure difference is opened when the valve is in the opening direction, and the pressure difference and Close the valve when it opens in the opposite direction. _ The above module is used to filter water. If necessary, a hollow fiber membrane is installed. _ It is also used to remove hardness when it is selectively rejected due to hardness. The water to be filtered flows through the tandem stages, and the permeate after filtration and optionally softening is collected from the outer surface of the diaphragm. The membrane permeability is about 0.1 gf d / ps i or more, and the total rejection is 80% or more. Minimum speed of flow / retentate through the diaphragm cavity _ between 0.15 and 0.6 ft / s. In various other aspects, the invention provides a reverse osmosis-or nanofiltration device containing a membrane module. The filter module has a plurality of leading or succeeding stages of the aforementioned hollow fiber membrane suspended between opposite heads. The module has a module feed inlet, a module retentate outlet, and a permeate outlet. The feed water path fluidly connects the module's feed inlet to a source of pressurized water, such as a well pump or tap water supply. An auxiliary pump can be used for pressurization if necessary. The permeate outlet is preferably connected to a permeate tank, such as a diaphragm tank or an air cushion tank, where the pressure and water capacity in the tank are ~

Page 11 508265 V. Description of Invention (6) Off. If the selected pressure in the permeate tank is reached, any feed side will be closed and the module retentate outlet will be closed. The minimum permeability of the diaphragm is 0, Ø, the minimum rejection is 80%, and the minimum hardness rejection is 70%. The minimum flow rate into g 'Psi is preferably between 0.15-0.6 ft / s, and more preferably 0 / wide retention ft / s. The feed / retentate passes through the module without recirculation. It is better to have a pressure drop of 3 to 30-12Opsi. In other aspects of the present invention, the formation of scale on the surface of the diaphragm and a method for reducing the scale are mentioned. Especially when using modules to provide softened permeate, osmium carbonate fouling may form in the membrane. To control fouling, appropriate f = agents, such as acids, or chemicals that generate acids in water, such as osmium dioxide = citric acid, to dissolve in liquid such as feed water, or carbon dioxide, == body , Spray into the module ^, inside the material / retentate side. The controlled cleaning chemical addition system can be used to spray fluid containing cleaning chemicals into the feed water, or the feed / retentate side of the module. In the continuous and simultaneous permeation method, the cleaning chemical is sprayed into the feed water continuously, and the device generates permeate. If the cleaning chemical is carbonized, the amount of carbon dioxide injected is best to make the feed Langelier scale. The 〃 exponent is zero or slightly negative. The two gasification carbons can be sprayed into the module only if necessary. In the discontinuous simultaneous infiltration method, J = chemical agents such as carbon dioxide are regularly sprayed into the feed water, and the device generates permeate. In another method, the direction of flow through the module is reversed, and cleaning chemicals such as carbon dioxide are added to the module from the retentate outlet at different timings. In the continuous but impermeable method, cleaning chemicals such as carbon dioxide are sprayed to the feed water substantially continuously, and the device does not generate permeate. Permeate

Page 12 508265 5. Description of the invention (7) The outlet is more fully open, allowing the feed / retentate to be flushed through the inner cavity side of the module to the drain port. During the suspend and flush method, the production of permeate was temporarily suspended, while the retentate outlet was more fully opened. The fluid containing carbon dioxide and other cleaning chemicals flows into the inlet of the module, for example, by spraying compressed carbon dioxide gas into the feed water flow that has passed through the inner cavity side of the inlet of the module. The fluid containing the cleaning chemical is taken to replace the feed / retentate in the inner cavity of the diaphragm until the substantial part, preferably all, of the inner volume of the hollow fiber membrane contains the cleaning chemical. The fluid containing the cleaning chemistry stops flowing, allowing the cleaning chemistry to react with the fouling _ The retention time should be selected. If necessary, the module can be rinsed with feed. Selection-The retention time is typically 1 to 30 minutes, or about 10 to 20 minutes. Rinse and dwell times are performed on a regular basis, for example, _-times per day when permeate requirements are low. In the gaseous cleaning method, the carbon dioxide gas is fed to the feed / retentate side of the module and replaces the feed / retentate side. The gas stays in the module for a while under pressure, and then flushes out with the feed water. The process can be repeated for additional cleaning. _ When referring to an increase in life in this case, it refers to an increase in the US system. Brief Description of the Drawings A specific example of the present invention is described below with reference to the drawings. Figure 1 is a partially cut-away elevation view of a filter module that can be used as a four-stage module; Figure 2 is a plan view of the beam group of Figure 1 with the top cap removed; 0 Figures 3 and 4 show the passage through the four stages Module forward and reverse flow;

Page 13 508265 V. Description of the invention (8) Figure 5 is an end view of another filter module; Figure 6 is a sectional elevation view of the filter module shown in Figure 5 along line AA of Figure 5; Figures 7 and 8 show the first and second end cap gaskets, which are used to define and separate the stages of the filter module of Figure 5;-Figure 9 shows the cross-sectional view of the inter-fiber partition plate of the filter module of Figure 5 ^ Figure 10 is a partial cutaway perspective view of the filter module assembly; / > 1 1 is a plan view and elevation of the collar used in the module of Figure 10. # 4 视 〜 ”Figure 12 Fig. 7 is a simplified diagram of the filtration system of the present invention; Fig. 13 is a graph of comparison of carbon dioxide consumption between different membrane cleaning methods; Fig. 14 is a graph showing the effect of residence time on membrane permeability during retention and flushing membrane cleaning methods Comparison graph; Figures 15 are graphs of the effect of the minimum feed / retentate velocity on the permeability of the membrane module. Detailed description of the preferred specific example of the module design " Figures 1 and 2 show multi-stage filter modules The general configuration of group 10. Module 10 has a plurality of filter hollow fiber membranes 12, suspended between opposite heads 14. The membrane is in reverse osmosis. Nanofiltration, preferably in the nanofiltration range, it is better to selectively detain the hardened maggots and the softened water of the permeate. The diaphragm 1 2 _ end 16 is installed in the head 14 in a closely spaced relationship, so that Its outer surface is sealed to the head portion 1, and the inner cavity of the diaphragm 12 is opened at the distal surface of the head portion 1. The first cap _

Page 14 V. Description of the invention (9) The septum cap 22 covers the peripheral surface of the head part 14 and is sealed in the head part Η. Ϊ 成 ϊ ΐ 成 ϊ: L4 群 ί i ϊ: Using the face of the first 14 without a diaphragm, you can "separate = ;; 2'4 inner bag"; Zhang towel = " partition plate 26 assembled in 2 (visible snow To open the 彡 轳 轳 9Π 90 times a towel (20, 22) (part of 22), extending from the cap 20 22 呷 face Ϊ face to seal contact with the head 14 without diaphragm 丨2 or all of us here. If necessary, the partition plate 26 can be inserted into the head portion 14 during installation. In the case of f, the partition plate 26 helps to fit the inside of the diaphragm 12 into the portion 14. Part or all of the partition plate 26 may be used; There are two: One-way valve 28 or above, such as a tongue valve. The configuration and installation of the diaphragm in the group 24 is not a work case. It is better to isolate the group 24 with redundancy, and reduce or eliminate the group. The outer periphery of the 24 spans is surrounded by the outer shell 30. The volume occupied by the Γ / 12 between the near end faces of the first part 14 forms the permeate chamber 32 ° permeate chamber M package, = = 12 surrounding space, and can also include the module 10 outer periphery. Adjacent open spaces are in direct fluid communication with the 4 group diaphragms 12. The fluid communication outlet 34 with the permeate chamber 32 allows the permeate to be removed from the module 10. Therefore, the water in the inner diaphragm of 浲 iii, 24 may be Directly flow to the product outlet 34 through the path of least resistance, instead of flowing through the group 24 in a selective way. This can be achieved by the diaphragm 12 being configured as a cylindrical fan segment, or other ^ = eg, in the In the square or rectangular module, there are 12 sets of barriers of various sizes = 丄 can be located on either side of the module's centerline. The module inlet 36 Feed into one of the covers 20, 22. The retentate leaving the module 丨 0 flows out from the module feed outlet 38, which is one of the fifth, invention description (10) cap, 20, 22. Brothers 3 and 4 show how the five groups e, separated by 12 (not shown in the figure), have four stages of flow in the former who should be the secretaries, ^, c, α. , And the branch water system flows in the first direction or in the reverse direction. And the diaphragm 12 group 24,6J in ", n, mf) is the stage of ϊΓ: ϊγ. The partitioning plate 26 is also in each leading stage; i ί = ;; Γϊ, 1 ′ Let the cap cover 20, 22 produce two movements, generally parallel to the periphery of the module 10. For example, in the case of the plume stage, the self-flow of the stage flows around the center of the module, although it is not necessary to have a perfect arc between the stages. The surface area of the diaphragm in each leading stage is between 1 and 2.5 times the surface area of the diaphragm in the subsequent stage, and the I® surface area of the stage decreases from the first stage to the last stage. The correct size of the selected stage 'provides a nearly uniform speed across the module 10, and although there are limited variations in the penetration speed between the stages, more or less other modules can be established. Modules of five to eight classes can be used for low feed pressure, for example, the feed is supplied by the household's tap water 'and there is no need to supplement the feed spring. You can also use ten or more modules, but you need to pay attention to the complexity of the modules. In module 10 in Figures 3 and 4, the group size is 1/8, 1/4, 1/4, 1/4, 1/8 of the total diaphragm size. The partition plate 26 includes a solid partition plate 40 and a one-way partition plate 42 at positions shown in the figure. The one-way partition plate 42 is open to allow flow in the direction shown. Partitions 26, 40, 42 divide group 124 into phases I, Π, Π, IV, depending on the direction of feed flow. In Figure 3, the material is fed through the module inlet of the first cap 20

Page 16 508265 V. Description of the invention (11) 36 'flows into group 24a. The feed also flows into group 24b, and groups 24a and 24b form stages]. Therefore, the module feed inlet 36 'in the first cap 20 is connected in fluid communication with the first end of the stage j. The feed / stagnation flows at the second cap 22 to the second end of stage I, where it flows to the first end of group 24c in section II. By the larger pressure in stage I (prerequisites for flowing from stage I to stage Π), the feed / retentate is prevented from flowing back to stage I through the one-way occluder 42. The feed / retained stream reaches the first stage. The second end of the cap stage ii 'flows here to the formation group 2 4 d first mountain,. The feed / retentate flowing to the second end of the stage dish flows to the second cap' here To the first end of group 24e forming stage IV. The feed / retentate flowing to the second end of stage '4 flows to the first cap 20, where it leaves the module 2 10 through the module outlet 38. Infiltration The material passes through all stages, and flows directly from the first #W section to the permeate chamber (not shown in the figure), and flows out through the permeate (through the X material and the mouth T). Phases i, n, m ′ IV are _, 1/4, 1/8 of the diaphragm. Li ^ / 8, In Figure 4, the feed and retentate flows are reversed. If it flows into the module 10 in the reverse direction, the liquid flowing through the mold is used as 10, and the groups of diaphragms 24, 26, 40, and 42 are assembled into a complex one-knife stage. . Specifically, the feed passes through the first cap 222 and the second outlet 38 and flows into the group 24e. The feed produced, and the group retentate. The trowel L entered the group 2 4 d, and was formed into phase I by 24d and 24e. The feed / retentate is in the stage ^ = cap 22 'then flows to the group of formation stage n / to the second feed / retained stream returns to the first cap 2 0, and Group 24b. The pole that flows in phase II, flows over to the formation phase II, and the detained material flows to the second cap.

508265 5 ~ Description of the invention (12) The cover 2 2 ′ flows here to the group 2 4a of the formation stage jy. The material / retained material in stage JY returns to the first cap 20, where it leaves the module 10 through the module feed inlet. Therefore, phases j, E, and Dish still involve 3/8, 1/4, 1/4, and 1/8 of the diaphragm's total interest, respectively. As described above, using the pressure and degree of jnm ^ = in some places can prevent the bad flow through the unidirectional partition plate M2 to change the direction of the flow through the module 10 and the feed to and from the module 10 The retaining pipe is provided with a valve, typically a solenoid valve, which allows each pipe to be connected to the module slave inlet 36 or the module retentate outlet 38. The valve uses the same operation of pLC or timer, so that the feed and retentate pipes will not be connected to the module at the same time. One point: the right module 1 〇 is used to soften the water, and the water to be filtered flows into the diaphragm, The first end of the cavity is selected for selective rejection, that is, restraint, which causes 21 kinds of hard sounds. The softened permeate is collected from the outer surface of the diaphragm 12, and the retentate is collected from the second end of the diaphragm f and flows out of the module 10 or to the next stage. The pupa of January hardness is accumulated in the inner cavity of the diaphragm 12, especially in the last stage, the feeding direction of the hollow fiber diaphragm is periodically reversed, so that the second ... The first uniform ^ = this scaling 'and extend the life of the module 10. In addition, despite the advantages of reverse flow, the module can also be used to construct a module for reverse flow only in one direction. The lifespan of the module is m, but it is more costly to construct "f", especially for small systems. Benefits. Figures 5-9 show the first module 11 〇, designed for unidirectional flow through four stages. The number of stages can also be used, and other shapes can be used. / 、 Absolutely >> Hollow fiber membrane 12 'Hanging between the first segment head 114a and the brother Yidaonu head 114b. As before, the end 16 of the diaphragm 12 is dense

508265 V. Description of the invention (13)

The spaced relationship is inserted into the segment heads 11 4 a, b so that its outer surface is sealed to the segment heads 11 4 a, b ′, and its inner cavity is on the peripheral surface 1 丨 7 of the segment heads 11 4 a, b. 119. The first end cover 112a (not shown) and the second end cover 12 2b cover the distal surfaces of the head portions 114a, b. A first tab 124 (not shown in the figure) is fitted between the first end cap 122 and the first segmented head 114a. In the same way, the second cymbal ία is set between the second end 盍 122b and the second segment header 114b. When the end cap 122 is tightened, a seal is formed between the segment heads 114a, b and the end cap 122. The outer periphery of each segment head 114a, b is sealed to the adjacent end cap, and a sealing chamber is defined for the first The two modules 11 〇 flow between the stages at each end. The thickness of the mats 1 2 4 and 1 2 6 is slightly larger than the minimum required to avoid the substantial drop loss of the flow between stages, so as not to unnecessarily increase the feed / retentate side volume of the second module 1 10. It is necessary to avoid unnecessarily increasing the volume of the feed / retentate side of the second module 110, which can help reduce the amount of cleaning solution required in some cleaning methods, as described later. However, for the large second module 11 〇, in order to avoid substantial drop loss during inter-phase flow, a thick gasket, a combination of gasket and spacer, or a hollow end cap 1 2 2 is needed to improve the stage Space available between rooms.

The first module 110 also has a casing 128. The auxiliary case 129 is fixed to the end of the case 128 and is provided with a thread for the end cap 122. Both the outer shell 128 and the auxiliary shell 129 have grooves on their inner faces to provide a stronger connection with the segmented header 114 which is positioned within the shell 28, 129. The central support tube 13o, which can be buried as required, can be buried in the second head section 1 14 to provide the strength and support of the second module 1 10. Peripheral 128 set permeate outlet 34. The central support tube 130 may also be porous between the segmented heads 1 1 4, whether extending from the second module 丨 丨 0 and communicating with the central opening of one of the heads 114. In this way, the permeate can pass through

Outlet 34 05. Description of the invention (14) Where there is permeate and it is discharged by the central support pipe 130, instead of the permeate in the shell 1 2 8 This can avoid drilling the permeate outlet and weakening the shell 1 2 8. The second module 11 0 with even-numbered stages allows all connections (feed, retentate), and is located at one end of the second module 1 1 0.

See Figures 6 and 9 for details. The heat sink 136 can extend longitudinally along the length of the central support tube 13o as required, enter the segmented head 114, and extend radially from the central support ^ 13 to the outer shell 1 28. This heat sink, as required, 3 6 & facilitates the installation of the cylindrical sector with the diaphragm 1 2, corresponding to the stages numbered 1 to 4. This project can also be achieved through support in the section header 114. It is also possible to fully install the diaphragm 12 without fins 136 or spokes, and rely on the stages defined by the gaskets 124, 126. However, the heat sink 136 or the spokes can make the membrane 12 easier to handle (for example, phase 1 is divided into two pieces for easy handling), reduce the number or convenience of random membranes 12 across stages, and count wasteful membranes 2 Minimized 'because one of its ends 16 is sealed with gaskets 124, 126. The heat sink 1 3 6 or the spokes also urge the stage to see the segmented head 丨 4 at the tip, which allows the gaskets 1 2 4 and 1 2 6 to be properly positioned relative to the stage without the need for an indexing mechanism. Furthermore, the spacers 124, 126 can be indexed to prevent them from being installed in the wrong direction. Figures 7 and 8 show the relationship between the first shim 1 2 4 and the second shim 1 2 6 and the stage. The center position of the heat sink 1 3 6 is shown as a dotted line. The ratio of the surface areas of the stages is 3.8: 2 · 4: 1 · 2: 1. Feed water inlet is drilled in the first end cap 122 &

Inside, after the first end cap 1 2 2 a is fixed in position, it communicates with stage 1. At the same time, a feed / retentate outlet (not shown in the figure) is drilled in the second end cover 12 2b, and after the first end cover 1 2 2 b is fixed in place, it communicates with stage 4. Figure 10 shows the components of the third module 4 1 0, and the design of the third module 4 10

Page 20 508265 V. Description of the invention (15) __ It is better for large modules, such as the diameter of 3 or 4 inches or more. After the diaphragm is installed, use the conventional polyimide chemical item f, which is slightly smaller than the diaphragm. 12, coated in the hollow fiber membrane 12; infiltration, especially before coating, the module must be completely dry, = ^ 〇, can not be dried at high temperature. Excessive drying can also cause cell loss and loss of sensitive permeability. In addition, formulating a stable polymer in amine applications = u 12 requires drying. The inventors have discovered that a large number of diaphragms are dry: if the diaphragm is contained in a module case. The diaphragms'd between the heads are especially small, and most of them are easy to achieve satisfactory drying. If necessary, large fibers are exposed to the air to speed up the drying process. The third module 410 of the human wind feather opening is composed of a plurality of (10 shown in the figure) components. The group element 41 1 contains a set of diaphragms (the pairs are not shown in the figure. The shape and size of each ridge makes the ridge 臈12 Slave: 12: I: More than 35M. Each element 411 can be individually coated with the first portion 414. The element 4 is Γ / together to make a composite for the third module 410. After installation, 1 can be f 1 Use the following procedure to install the third module 410. δ is silly. You can coat the components 4 1 1 compartment + eight membranes 12 separately, and then apply the component 411 to the knife and the two helmets. Module 11〇, gaskets and end caps (in the figure, the third module is combined into the third module 410. One ^ Α] 〇 ± ^^ is not attached) is attached to the end of the third mold 1 410 'the diaphragm The composition phase. The natural separation between the shafts. If the separation is needed elsewhere, slide the blocking plate 442 into the -pair or multiple pairs of collars "0. Because: in ㈡;

508265 V. Description of the invention (16) 440 The size is considered for coating (especially drying), but the number or size of stages is not limited by the size or number of the collar 4 4 0. Making the third module 4 1 0 with a single size and shape of the component 4 11 can create coating and installation tools and techniques, which help to produce a uniform third-quality module 4 1 0. Especially when a large number of collars 440 are used, the gasket can be easily made into a multi-stage third module. For example, in the case of the use of eight collars 44 in each composite head 41.4, a fourth module can be generated using a third module, as shown in Figures 1-4. Using spacers and a partition plate, the partition The plates 40, 42 are shown. The manufacturing method of the third module 410 is detailed as follows. The third module 41 shown in the figure is about 35 inches long between the ends of the composite head 4 1 4 and uses an 8-inch diameter gray PVC pipe as the module case 4 3 0. Each of the plurality of headers 41 4 is composed of 10 collars 4 4 0. The pair of opposed collars and the diaphragm installed therein form 10 elements 4 1 1 each containing approximately 1 60 0 with an inner diameter of approximately 0.4 mm. Hollow fiber membranes (not shown). Each element 4 1 1 is assembled in a mold, and the distal surfaces of the pair of collars 440 are kept separated by about 35 inches. The diaphragms 12 are held together at their ends by rubber bands or other straps so that they can be inserted into the collar 440. The diaphragm 12 bundle is held on the die by another rubber band or band, and the die is flat on the table. The diaphragm was then cut so that it protruded beyond the distal surface of the collar 44o approximately i inches. The mold returns to its upright position. Closing the fiber end 'A small dish or polysilicone in the cup about 5mm is brought to the bottom of the fiber. Polylithium oxygen rises to about 10 mm in the fiber and surrounds each fiber. Drain any excess. Once the polysiloxane is fixed to no flow, the mold is turned over and the replication process is repeated on the other side. T is the installation element 41 1 and all 10 components 4 1 1 are placed in the installation mold to form two composite heads 4 1 4. Install the mold into two halves, so the component 4 1 1 can

Page 22 Country II

508265 V. Description of the invention (17) Put in half of the ϋ lifter, leaving a proper space between the end of the mold and the distal surface of the collar 440. Appropriate temporary spacers can be placed between adjacent collars 440, or within 70 pieces 41 1-between pairs of collars 440 to keep the collars 440 and diaphragm 12 positioned. Once all το pieces 4 1 1 and any spacers are installed in the second half of the installation mold, the two halves can be clamped at =, so that the element 41 丨 and the spacers are tightly squeezed into position. ^ The combined mold is placed in the centrifuge. The centrifuge is equipped with a pouring mold 'to eject resin through one or more ports. The resin can be applied to both ends at the same time, or a small amount to the end of rotation until the full amount is shot. The centrifuge was rotated at about 300 rpm, and a force of not less than 40 G was applied to the resin. The resin is fully cured until it does not flow. The centrifuge is turned off and the mold is removed. However, it is best not to remove the three modules 4 1 0 from the mold until the resin is fully cured. The resin can also be injected statically (without centrifugation) into each end of the installation mold. One end of the module is rotated 180 ° to install the other end. Once the resin is fully cured, the element 411 is removed from the mold, but is still stuck together with a thin layer of resin. For example, cutting in a band saw removes resin from the end, revealing open fiber ends. The band saw blade should be cut through the resin just at the tip of the collar 44o to leave enough resin to keep the collar 4 4o together while cutting, but to allow the elements 41 1 to be easily separated from each other. After the gadolinium elements 411 are separated from each other, a temporary cap is put on the circumference of each collar 4440, and each of them is tested for its integrity and initial permeability. In the integrity test, the bubble point septum 12 was cut and sealed with silicone. These test caps can be used for leak testing, ruggedness, coating, and rejection / penetration testing. To coat the separator 1 2 ', it must be dried. To do this, remove one of the covers and allow any excess liquid in the fibers to drain. The inner cavity is filtered with ΗΕ =

Straight 12 winds, the membrane steps into the cover in a row, and the cap ring test or test gas passed his test (18 gas to more bright nitrogen in addition to | or f f9 milk). 12h. I empty wet ml ^ J box inch 2 about 1 degree thick to dry, separated by a few inches to make the clock feel dry, if you want to touch 30 if you need to touch about 12 fans, the film wind consumption is 11 Separately, 4 r continued coating with amine solution, followed by drying as described above, and then applying organic solvents ^ and then dried as described above. Both solutions were pushed into the membrane with nitrogen 1 2 inside two 'using the test end cap to maintain the cavity After the required time. 总 After coating the internal cavity, the total membrane 12 can be rinsed with water on the outside, immersed in a 30% glycerol solution to save the fiber, and then further dried as described above. After the element 4 丨 丨 is air-dried, Into the flood box. Once the element 411 is dry, the test end cap can be replaced. The element 4 1 1 is tested for permeability and rejection. The element 4 丨 immersed in glycerin and dried again. The elements 411 can be adhered to each other. And into the module shell 43. In this example, it is a gray-level 40 pvc pipe. The filtering method is shown in Figure 12. The filtering device 300 is suitable for use at the entrance of private houses, small groups of houses, or small commercial buildings. The device 300 can be used to remove suspended solids, and it can be determined as needed. The sclerosis that causes hardness is filtered and the permeate is softened as required. The device 300 includes a slag module 336, which has a feed water inlet 334 for introducing feed water, and a retentate outlet 338 for removing retentate, And the permeate outlet 348 to remove the permeate after the treatment. The filter module 336 can be various types of nanofiltration or reverse osmosis modules. 'It is filtration and technically known. For example, the filter module 3 3 6 can be spirally wound. Nanodiaphragm module, or an assembly of the module, or a plurality of hollow fibers

Page 24 508265 V. Description of the invention (19) The diaphragm ′ may be in accordance with one of the aforementioned modules 1 0, 1 1 0, 2 1 0 or 41 0. The feed water passage 310 is a feed water inlet 334 fluidly connected to the filter module 336. The device 300 further includes a cleaning chemical addition system 316 for injecting one or more cleaning chemicals into the feed & channel 3 10 upstream of the filter module 336. The cleaning chemical addition system 3 1 6 is operable to supply a fluid 'containing a cleaning chemical into the feed water path 310. The fluid can be a liquid, such as a lemon " acid or a carbonic acid, or a gas, such as a carbon dioxide gas. Ding

The cleaning chemical addition system 3 1 6 can take many forms. If the cleaning chemical is a liquid, such as citric acid, use various mechanisms, such as a metering pump or storage tank connected to a venturi tube in the inlet + water, path 310. If the cleaning chemical agent is carbon dioxide gas, or a # acid made by dissolving carbon dioxide gas in the feed water, the cleaning chemical agent adding system 3 1 6 can be as shown in FIG. 12. In the i / graph, the pressurized cylinder 317 is adapted to hold food-grade compressed carbon dioxide gas. The carbon dioxide path 318 connects the carbon dioxide cylinder 317 to the filter module 336 and is fluidly connected to the feed water path 310. The carbon dioxide path 318 is connected to the inlet f = 310, and the connection point 310 is preferably Λ and Λ which are favorable for the carbon dioxide cleaning. / Nine 317 downstream may contain carbon dioxide pressure regulation; 1 volume controller 324 to help maintain the appropriate gas carbon dioxide valve 326 between the water 310 and the circuit, preferably the solenoid valve switch. The second slave valve 32 6 can be connected to one because of the following cleaning systems

ΐΠΐί or? Force detector. If carbon dioxide is to be used in the solution > monthly washing, the cells can be stabilized with Rensi Er rolled carbon foaming facility 325, and carbon dioxide is introduced into the feed water to achieve rapid dissolution of carbon dioxide gas. two

Page 25 508265 V. Description of the invention (20) Oxidized charcoal bubbling facilities 3 2 5 may be composed of a porous hollow fiber membrane, or a ceramic porous bed or a packed bed with ceramic or stainless steel packing materials. It is preferred to include a pre-filter 3 1 4 with appropriate filter media and activated carbon columns, which may be upstream of the transition module 336. The filtering medium removes particulate matter, which is typically particulate matter having a diameter of about one-tenth of the inside diameter of the membrane 12. Activated carbon columns are used to monitor relatives, and L " uses one or more pre-filter pressure transmitters 338, if necessary, to feed water pressure, and drop loss through pre-filter 314.

Into Psi. The feed water of the filter module 336 is pressurized to a pressure of typically 40 to 200. Not shown: The feed water source can be a pressurized tap water supply line 3 1 0 or a well pump (the picture shows In order to pressurize the 1 water supply line, the pressure that can be contained in the device 300 is set Γ the pump 330 upstream of Ertian Bu to increase the feed water inlet 334. Supervise the filtering mode: Γ36 = 346 'stagnation, go to the road except 34d, stay: do not The outlet 338 is fluidly connected to the discharge. The retentate passage 34n ^ = I valve 342 is stopped and started, preferably a solenoid valve. The pore path 340 also contains the retentate flow control system. Stagnation, variable area flow pores or _Door-making mechanism 3 uses, for example, a permeate made by a mobile device to induce control, especially] t, advance in the absence of permeation 2 = / can be used for cleaning * method, such as Jinke ΐ ΐ need to keep the required minimum When the feed /, m-holding J belt is kept at a low flow rate, the difference between the force and the pressure of the permeate is to reduce the material velocity (detailed later).

Page 26 508265 V. Description of the invention (21) The permeate channel 3 50 is fluidly connected to the permeate outlet 348 of the filter module 3 3 6. The permeate channel 350 can be directly connected to a permeate distribution system or a buffer tank, and a tank in which the pressure in the tank increases with the increase of the permeate volume is preferred. For example, downstream of the filter module 336, a diaphragm groove 362 having an inlet 360 may be used. The pressure transmitter 361 can monitor the pressure in the diaphragm groove 362. The device 3 0 0 may also contain a system bypass valve 3 5 6 located downstream of the filter tank group 3 3 6 to isolate the user from any permeate that may be generated during cleaning or module failure, replacement or maintenance. If the system bypass valve 3 5 6 is closed and the bypass valve 370 located in the bypass passage 368 is opened, the bypass passage 368 is fluidly connected to the feed water passage 3 1 0 and the permeate passage 3 5 0.

The device 300 detains suspended solids, which may contain pathogens, heavy metals, or plutonium that causes hardness, and produces filtered or softened permeate as needed. In the filtration, the valves 3 1 2, 342, 356, 35 8 are opened, and the bypass valve 370 is closed. Initially, the 'feed water passed through the feed water passage 3 1 0. If necessary, increase the feed pressure at the feed water inlet 334 with fruit 33 \. Therefore, the pressurized feed water should reach the feed side of the module 336, the permeate is collected when it leaves the outer surface of the diaphragm through the permeate outlet 348, and the concentrate or retentate is continuously passed through the retentate outlet 3 at the permeate boundary. 3 8 left. The filtered permeate travels / passes, and participates in the permeate passage 350, and may enter the pressurized diaphragm tank 362, or directly to /

The user ’s choice depends on whether a pressurized diaphragm tank 362 (or other similar tank) is used, depending on the amount of permeate required. The retentate flow is controlled using the retentate mechanism 344. Within industrial and commercial facilities, the device 300 typically = operates in a substantially continuous manner. However, operation depends on design parameters, ^ 1 parameters, system capacity, and system requirements. Device 300 can stay pack 1

508265 V. Description of the invention (22) A flow transmitter 352 is located downstream of the filter module 336 to monitor the permeate production ’and a conductivity sensor 354 is provided to monitor the integrity of the system.

In one embodiment, the 'device 300 is used to provide transition and softened water for a single house. The filter module 3 3 6 is a multi-stage module 10, 丨 丨 41, as described above. The diaphragm 12 has the lowest permeability of 0.1 gfd / psi and the lowest hardness rejection of about 75%. The filter module 336 has a membrane surface area of 100 to 5000 square feet and is divided into 5 to 8 stages, preferably 6 to 8 stages. Filtration is performed in a single pass with no retentate recirculation at a low minimum feed / retentate rate and high recovery. The lowest feed / retentate rate is typically between 0.15 and 0.6 ft / s, and more typically between 0.2 * 0.03 ft / ^ a1. The feed pressure is between 60 psi and 150 psi. This pressure allows tap water to be supplied to the home, using only a pump 3 3 0. In this specific example, the 'device 300' is typically operated for 1 to 6 hours per day, and more typically for 2 to 3 hours per day. Filtering is controlled by a program logic controller or a tank pressure transmitter 361 which is operated by a circuit of various valves (not shown in the figure). The two tank pressure transmitter 361 promotes filtration to start at a selected minimum pressure, The pressure stops. If the filtration is stopped, if any pump 3 3 0 (or well pump) is used, it is stopped, and valves 342 and 3 58 are closed. The permeate passage 350 may be in communication with a domestic supply line (not shown). However, diaphragm grooves 362 are best used. The device 300 can be operated for an extended period of time, but the inlet water flow is between 0.5-5-7 gallons per minute, and more preferably 丄 to m per minute. Therefore, the diaphragm tank 362 is used to store processed permeate Until the user needs it. Diaphragm slot 3 6 2 is fluidly connected to via slot inlet 3 6 〇

508265 V. Description of the invention (23) f permeate channel 350. Migrating in the pressurized diaphragm tank 362, the permeate passage 35 is introduced into the home supply line. Diaphragm tank 362 can hold 5 to 100 gallons of water, 30-70 gallons on the type A, and more typically 50-60 gallons. 8. Cleaning Washer In order to provide cleaning, reduce scaling, and extend the life of the reverse osmosis or nanofiltration module, the following describes various methods to provide the cleaning chemical curtain module. These methods are particularly useful for making softened permeate using modules, and cleaning chemicals can also be used to control scaling. In order to reduce the fouling of carbon dioxide, the agent is preferably an acid, or a substance that generates acid in water.

Examples of cleaning chemicals include citric acid, which can remove scale and effectively remove some metals. Carbon dioxide can also be used, and it is surprisingly effective to remove the fouling of carbon dioxide. Carbon dioxide can also limit very hard water with buffering capacity, that is, excessive doses will not cause extremely low pH and potentially unsafe water quality. In addition, food-grade carbon dioxide is suitable for human ingestion, can be compressed gas cans, and can be used for personal use in domestic facilities. The pH of the carbonic acid applied to the module is between 4 · 5 and 6 · 5 ', typically between 5 · 0 and 6 · 0. The citric acid applied to the module is typically between 2 · 5 and 3 · 0. ~ Various cleaning methods can be used to clean the filter module 336 and reduce scaling. In the continuous simultaneous infiltration method, the 'cleaning chemical adding system 3 1 6 is opened, and the cleaning chemical is continuously filtered. If the cleaning chemical is carbon dioxide, the monoxide reverse valve 3 2 6 is connected to the tank pressure transmitter 3 6; [, to open the valves 342 and 3 58 that should be opened, that is, when the minimum pressure is selected, and when the maximum pressure is selected Stopped. The carbon dioxide flow controller 324 is set at a flow required for the introduction of carbon dioxide. CO2 pressure regulator 320 and CO2 flow controller

508265 --- V. Description of the invention (24) 3 If 24 is set in advance, it is suitable for various operating conditions ^ ~~ t is necessary, the carbon dioxide pressure regulator 32 field is preset, a single set value σ 4 can be combined to respond to the feed Absolute u — Poor oxidation flow control force difference, or one of the permeate flow or the force, the pressure between the feed and the permeate is nearly constant carbon dioxide injection rate. In order to provide each volume of feed water, more cleaning chemicals are added. In the expected service life of each piece of equipment, the diaphragm is scaled up to make it in between. It can have a full reading of Angstroms, between 1 and 6. Months and 1 year, the sound peak X μ »is less. At the end of this period, the kick can be removed ... For example, you can add a two-negative town ”Chen Yunzhi Mi Mi slightly negative number, at this point, the feed water does not have | the ancient index is zero or: clever. Carbon dioxide turns insoluble carbon: tritium; rotten calcium bicarbonate. In this way, adding _ 4 π # ^ =, ·, α scale is converted to solubility: and: low scale formation rate. The excess of the remaining two in the feed water. Membrane: 3. The scale membrane that has been scaled ® ′ restores at least-part of the membrane permeability. Since the concentration of 塩 that forms the scale increases in the later stages of the multi-stage filter module ^ 3 6, it is not necessary to worry about the formation of scale in the initial stage or several stages of the filter module 336 ^ R τ Keren. In this case, the carbon dioxide pathway can be repositioned to feed the feed directly to the filter module 336, upstream of the later stage, or just upstream of the final stage, and less carbon dioxide can be used. The carbon dioxide path 3 丨 8 is divided so as to inject carbon dioxide into the feed water path 3 1 0 and the filtering module 3 3 6 upstream at a later stage. In the case of discontinuous and simultaneous infiltration, cleaning chemicals are periodically added to the feed water. For example, every 1 to 3 hours, carbon dioxide can be added for 5 to 30 minutes. This is the continuous operation of the filtration system 3 0 0, the carbon dioxide valve 3 2 6

Page 30 V. Description of the invention (25) Connected to timer or microprocessor ^ If the filter system is not a continuous transmitter 3 6 1, so when the valves 342 and 358 are closed, the timer or microprocessor is closed. (Shown on the machine chart). If the valves 342 and 358 are opened, only the tank pressure transmitter 361 is early, so the carbon dioxide valve 326 is closed. That is, other cleaning methods are often performed when ^ p, Θ H M is suspended when the penetration is stopped. These methods are typically 疋 ° one by one ’column * as in a continuous operation business system, every 1-

1 Λ’ΛνΛ Wash for 10-30 minutes to inhibit fouling, and remove ΐ ΐ,> month: ί: A small amount of fouling has formed. Cleaning can also be done at longer intervals, once a day on the mother's case, but each cleaning provides stronger descaling. It can be washed once every day, especially for residential use. It can be used when the water demand is often low, such as 2-4am. Generally speaking, the frequency and intensity of cleaning depends on design parameters, operating parameters, and system capacity. , And depends on the needs of the system.

-In a continuous but impermeable method, a timer or microprocessor (not shown) starts the cleaning step at a selected time. The permeate valve 358 is closed, but the retentate valve 3 4 2 is still open and the feed continues to be supplied. Operate the cleaning chemical addition system 3 1 6 and introduce the cleaning chemical into the water flowing through the feed / retentate side of the filter module 3 3 6. For example, in the case of carbon dioxide, open the carbon dioxide valve 3 2 6 to introduce carbon dioxide into the feed flowing through the feed / retentate side of the filter module 3 6 6. If the retentate flow control mechanism 3 4 4 can be changed, it can be fully opened shortly after the cleaning starts to accelerate the flow of carbon dioxide into the filter module 3 6 6 until the carbon dioxide extends through the module. The retentate flow control mechanism 344 and / or the carbon dioxide pressure regulator 3 2 0 or the carbon dioxide flow controller 3 2 4 can be adjusted to provide the required concentration and contact time of the carbon dioxide.

Page 31 508265 V Description of the invention (26) ___ In the pause and flush method, the blind is to start the cleaning step at a selected time: n ^ 2 = (not shown in the figure) also continues to flow. The retentate valve 342 is briefly opened, and the main valve 58 is closed, but when the feed material 316 sprays cleaning chemicals into the filter = ^ first chemical agent addition system, the retentate is flushed out of the module 336. In the second example, the same valves in the feed water of 1 336 remain open until the dihydrogen iodine > & carbon monoxide valve 326 is opened. The second material / retentate side, preferably at least 丨 the filter module 336 most of the retentate 阙 342, which is allowed to pass the module ㈣ After the carbon dioxide valve 326 is closed, the pressure on the retentate side rises. Water keeps 60 minutes in the filter module; ', water), force. With the addition of dioxide, the acid reaction is slower, and when paused = time, the device 300 returns to worry, and control returns to the tank pressure transmitter 36. Before resuming the filtration, the retentate valve 3 4 2 is briefly opened to allow the feed water to flow through the filtration module 3 3 6 to flush the contents of the filtration group M 3 3 6 out of the device 3 q q. This step is not typically necessary because the carbon dioxide is essentially used up. In addition, in the above-mentioned residential system, the cleaning is performed outside the peak time, as described above, water is immediately needed and any remaining carbon dioxide simply continues to react with the fouling. 'Used in another cleaning method' Cleaning the filter module 3 3 6 by keeping pressurized carbon dioxide gas on the feed / retentate side of the transition module 3 3 6. Refer to Figure 12 for cleaning chemical addition system 3 丨 6 as shown, but no carbon dioxide bubbling facility 3 2 5 is required. To perform this cleaning method ’, first close the feed valve 380 and the permeate valve 358,

Page 32 508265 V. Description of the invention (27) _, the filter module 3 3 6 is supplied from the feed, = 326 and the retentate valve 342 is opened for a period of time ^ away ^ rolling f is substantially discharged into the filter module 336 Material / retentate. One oxidized oxygen © Z is discharged from the feed / retentate side of the 遽 module 336 and the entire feed is discharged. The other part of the feed / retentate side of the 336 is used, and the surface tension is taken into consideration. except. The node controller 32 adjusts the range of kPa to 1 (kPa), typically 10-50 kpa. One J = ^ Exhaust 'retaining matter_2 and carbon dioxide 326, ie, the filter module 336 of 填 / stagnation = body is left standing for 40 minutes, typically about 15_3 ^ Xu Chong', while carbon dioxide is related to the formation of scaling compounds reaction. ^ L Γ / ΛΥ / 42 5 '; t ^ ^ ^ ^ 336 ^ 33B ^; 10 times flushing of the volume of the inlet / retentate side, 1-2 times its volume, closing the feed valve 380 and the retention valve 342 One of them, stop flushing. Second ', the back stone is suspended in the filter module 336, and then rinsed with the feed water. The cycle is repeated 1 to 5 times, depending on the degree of fouling. When using this cleaning method as maintenance cleaning, if the filter module 336 has been scaled up to about 80% of its initial permeability, the cleaning is performed. Typically 1 or 2 cycles are sufficient. Under the main strategy, if the filter module 336 has been scaled up to its initial permeability of about =% ′, it is cleaned, typically requiring 2-5 cycles. 0 In the flush and pause methods, the gaseous carbon dioxide cleaning method essentially requires less carbon monoxide to dissolve into the feed water. Gein II—Carbonide is only dissolved in the cells of the membrane 12 or in the water held on the surface. For example, in the experimental filtration system, about 500 hollow fiber spacers with a length of about 1 meter =

508265 V. Description of the invention (28) 12 For the test filter module 336, the flushing and suspension of the cleaning carcass dissolved in the feed carcass typically require about ^^^ carbon dioxide gas to allow the carbon dioxide gas to directly enter the filter module 3 3 6 t quasi-litre, while washing cycle, only about 0.07-0.1 standard liters per cycle? Wash and pause wash results. In a commercial specific example, the present inventors predict that the difference will be less, but the use of carbon dioxide in the flushing and suspension method is poor. The carbon dioxide dissolved in the feed water is used for flushing. And the suspension body is still only about half the carbon, and the approximate cleaning result is obtained. The required dioxide is obtained. Operational considerations and the cost of control equipment are beneficial to the carbon dioxide in some specific examples, but in other cases Direct transmission and use of feed water are beneficial to reduce carbon dioxide consumption. Carbon monoxide gas The above-mentioned methods can be used in combination, for example, to provide a long-term agent in the feed, while infiltrating, and when the infiltration is stopped, = f plus cleaning chemical scale. The above method can also be combined with the above flow inversion, = j, when the force is removed and the inversion is reversed, the module 10 of its stage can be reconstructed. 22 = j For the flow feed, the supply of washing chemicals can be switched between the addition of 〇if and the outlet of the module and 338 of the module. 枓 Here; the initial and final stages of feeding, cleaning chemicals Alternately, the lower hard J water with higher concentration and the higher hardness water with lower cleaning chemical concentration alternate, and the cleaning chemical concentration decreases as it passes through the module 336. Therefore, the cleaning chemistry is added to the stream, and the feed stream has the most serious fouling in the mold at least immediately after the flow is reversed. When the cleaning chemicals are added periodically, the reverse flow can only be periodic, and the time is consistent with the time when the cleaning chemicals are added to the feed. Therefore, most

508265 5. Description of the invention (29) During the days, the feed material flows in the forward direction, and the fouling is accumulated in the final stage. During off-peak periods, the flow is reversed, and cleaning chemicals are added to the feed. Therefore, cleaning chemistry is added to the feed stream, and the feed stream enters the most fouling part of the module first. Example 1 The graphs in Figures 13 and 13 compare the carbon dioxide consumption of the two cleaning methods performed by stopping the infiltration. The first method is a continuous but impermeable method, and the second is a pause and rinse method. The y-coordinate is related to the permeability restoration, and the X-coordinate is related to the carbon dioxide consumption in pounds (1 b). Solid diamonds and solid squares indicate the second module to remove scale in a continuous, impermeable method. Hollow diamonds and hollow squares indicate the same two modules to remove scale during the temporary and flushing methods. The synthetic feed solution was operated at a feed pressure of 100 psi, a temperature of 7-10 ° C, and a retention flow rate of 0.19 f t / s for 16 hours to foul the diaphragm. Cleaning conditions include: · Inlet #pressure 1 OOpsi, temperature between 20-25 ° C, industrial water feed is filled with carbon dioxide bubbles, pH is between 6.0 and 5.5, and the rate is 0.6 4 ft / s ( In the case of rinsing or continuous and non-osmotic cleaning), the rinsing time is 1 minute, the pause time is 1-40 minutes, and the flow time (in the continuous and non-osmotic method) is between 5-30 minutes. The characteristics of the two modules are slightly different, which are summarized in the following table: Factory ~ r " —--Γ-π 1 Diaphragm properties 1 Module AI Module B 1 1 1 (shown in diamond) I (shown in square) 1 h -+--+ ---- -H 1 surface area (m2) 1 0. 804 | 0.801 1

Page 35 508265 V. Description of the invention (30) r — s__ h sectional area (m2) + I +

1 Permeability (L / m2 / h 丨 I / bar) I Bu ————__——- | — I Total hardness rejection (%) I .8 6 E-5 3. 75

Η0.85E-5 I 4. 08 I + Η 70 · 4 74 The ancient two methods can successfully descale the module. However, the general trend is that the carbon dioxide and rinse processes require far less carbon dioxide than continuous processes. Separate I 1 through 4 Ϊ 2 3 line diagram, compare the pause time with the flush time method. The benchmark system is about the pause. The y-coordinate system is about the percentage increase in permeability. The x-blocks all use synthetic concentrated solution 3 in minutes. In these experiments, the maximum $ pb ^ hardness i 20011 ^ / 1 of all the diaphragm stage modules was simulated with CaC03 solution for many hours. Each data point table ^ ^ ′ is operated at a recovery rate of 80-90%, and the amount of fouling is increased by 16%. Diaphragm = Permeation temperature reached after consuming 0.003 pounds of carbon dioxide, about 7-1 (rc, = test conditions include · feed pressure 100 psi '0 · 19 ft / s. =: Synthetic feed solution, outflow rate • 0, outflow includes industrial water and carbon dioxide, ρΗ at, τ time between 1-40 minutes, · 6 4 ft / s, rinse time 1 minute, The above table shows the graph; the second module with different characteristics :: fruit: the marginal increase in the rate of decline in the penetration rate, _ page 36 508265 5. Description of the invention (31) The time is about 15-20 minutes. Example 3 The graph in Figure 15 shows the effect of the feed / retained flow rate of the single-stage filter module on the permeability of the filter module. The y-coordinate refers to the permeability, the unit is L / m2 / hr / bar, and the X-coordinate is Flow rate in ft / s. Test conditions include: module pressure 100 psi, temperature between 25-30 ° C for 4-6 hours, synthetic feed solution 12 20 mg / l, total The hardness is calculated as CaC03, which simulates the last stage of a multi-stage module and operates at 80-90% recovery rate 3. The test includes three different sizes The module details are as follows: I diaphragm performance module A (diamond) \ ~ ——————- 1-- Surface area (m2) | 0.808----- | ____ Sectional area (m2) I 8 55E-5 +-I Module BI (square) Module c (Triangle ———-_ h + — __ ........- _ ___I π ---- ~ ~ I 0 · 797 I 0.621-] ------ I_____ I ---- ~ I 8.48E-5 I 8.16E-5

Permeability (gfd | 0.097 / psi I bu ll one one one-I____ one total hardness rejection I 88 (%) I + + .149 79 Η— 〇. 122 Η 81 — — one --- 1 --- --j _____ The graph shows that the outflow rate exceeds about 0.2 ft / s (for the lowest feed

V. Description of the invention (32) _ ;; ΐ rate; Λ '/ Λ rate increase on the permeability of the diaphragm does not show any day and month 1 fast scale. Below about Q.15 ft / s, the permeability decreases. Examples of the series "《^ Testing, using a coating with an inner diameter of 0 · 5mm is slightly over Γ: use :; select t rejection (ie detention) The causes of hardness are: test H Ξ Ϊ 臈 f filtration and softening the total hardness of more than 3 ° 0 ° 11 ^ 1 extremely hard and the company, after 6 hours of water immersion operation, the diaphragm flow significantly reduced to various types And the range = degree P. 3-the carbon oxide solution is circulated through the diaphragm. There were two defects in the test, and the flow rate of the diaphragm can be fully recovered. ^^ Example 5 Two sets of Desal DL 1812 spiral wound nanofiltration modules were operated at a recovery rate of 50 and approximately 99 psi TMP. The feed has a scale-forming property and the Ryznar index is positive. Carbon dioxide was continuously injected into the feed of one of the modules, and the pH dropped from 8.0 to 6.5. The flow rate of the module fed without carbon dioxide is stable at 0 · 20gfd / psi. The flow rate of the module added with carbon dioxide was stabilized at 0.26gfd / psi, an improvement of 30%. " Example 6 Carbon dioxide gas was used to test a nanofiltration module using a hollow fiber membrane. The module has about 600 fibers, an inner diameter of about 0.4 mm, and a total surface area of about 0.8 πί. The module is used to filter the feed water, and its total hardness conversion cac0 is between 1 500 and 1 700 mg / l. The lowest feed / retentate rate in the fiber is about 0. m / s. Close the valves on the feed and permeate lines for cleaning. Connect the pressurized carbon dioxide source to the retentate discharge line and open the drain valve on the feed line.

Page 38 508265 V. Description of the invention (33) The carbon dioxide gas is used to discharge the feed / retentate in the module. In a module with a pressure of 5OkPa, carbon dioxide gas can be maintained for 20 minutes. Rinse the module with low hardness water. The cycle of pressurized carbon dioxide and flushing the module is maintained in the module, and it is repeated twice more. The module returns to the service ranks. The initial permeability of the module is 2.8 L / m2 / hr / bar. After filtering for a period of time, the permeability of the module is 2.4 L / m2 / hr / baar. After cleaning with carbon dioxide gas, the module permeability is 2 · 8 L / m2 / hr / bar. Therefore, carbon dioxide cleaning can successfully restore the module to its initial permeability. Example 7

Module with hardness rejection nano-filtration membrane, surface area of 0.76 m2, total hardness rejection of 76%, baseline permeability of 2.11 L / m2 / hr / bar, scaled up with a synthetic solution of hard water. At the end of the fouling period, the permeability of the measuring module is 1.6 65 L / iri / hr / bar. The module is then rinsed and suspended with a carbon dioxide solution in a hard water synthetic solution. The flushing flow is 2 to 3 times the capacity of the module feed / retentate side, and the pause time is 20 minutes. After cleaning, the module permeability was measured using a synthetic solution of hard water at 192 L / m2 / hr / bar. At the same time, the mold group was fouled by the hard water synthetic solution, and the module permeability was t · t L / lrf / hr / ba: f. The module is then flushed and suspended with carbon dioxide gas. The pause time is 20 minutes. After cleaning, use a hard water synthetic solution to measure the module permeability to 184 L / ni / hr / bar.

The above specific examples may have various modifications within the scope of the present invention, as defined by the following patent applications.

Page 508265 Brief description of the drawings. Figure 1 is a partially cut-away elevation view of a filter module that can be used as a four-stage module. Figure 2 is a plan view of the module in Figure 1 with the top cap removed. Figure 4 shows the forward and reverse flow through the four-stage module; Figure 5 is an end view of another filter module; Figure 6 is a cross-section of the filter module shown in Figure 5 along the line AA in Figure 5 Figures 7 and 8 show the first and second end cap gaskets used to define and separate the stages of the filter module of Figure 5; Figure 9 shows the inter-fiber partition plates of the filter module of Figure 5 Sectional view; Fig. 10 is a partial cutaway perspective view of another module component; Fig. 1 A, Fig. 10 Plan view and elevation perspective view of a collar used in the module: ½: more? Y12th Figure ^ Simplified diagram of the filtration system of the invention; Figure 13 is a comparison curve of carbon dioxide consumption between different diaphragm cleaning methods; Figure 14 is a comparison curve of the effect of residence time on the permeability of the diaphragm in the retention and flushing diaphragm cleaning method Figure; Figure 15 is a graph of the effect of the minimum feed / retentate velocity on the permeability of the diaphragm module.

Page 40

Claims (1)

508265 6. Scope of patent application 1. A filter module, including: (a)-opposite heads; (b) a plurality of hollow fiber diaphragms installed in the head, so that the inner cavity of the diaphragm is opened to the distal surface of the head; (c) housing Extending between the heads, there is a permeate outlet to define-the permeate collection chamber, which is in fluid communication with the outside of the diaphragm; (d) — caps or caps, which are fitted over the heads, caps (i) Surrounding: the peripheral surface of the head, (ii) contains one or more separator plates to divide the diaphragm. Multiple successive stages, each stage has a first end and a second end, the inner cavity of the diaphragm is here-in fluid communication with the cap; And (iii) provide a fluid connection for fluid flow between the second end of each leading stage and the first end of each subsequent stage, the direction of which is generally parallel to the outer periphery of the module; * (e) the module inlet, and the first The diaphragm cavity in the stage is in fluid communication at the first end of the first stage; and (f) the module outlet is in fluid communication with the diaphragm cavity in the last stage at the second end of the final stage. _ 2. If the module of the first patent application scope, the surface area of the diaphragm of each leading class is 1 to 2.5 times the surface area of the diaphragm of the subsequent stage, and the surface area of the class is from the first stage to the last. Decreasing stage. 3. For the module of the scope of patent application No. 2, in which (a) the partition plate is equipped with a valve configured to enter the module retentate outlet when the feed water flows into the module in the reverse direction, and the partition plate (i) The diaphragm is reassembled into a second leading and second succeeding stage having a first end and a second end, the inner cavity of the diaphragm is opened to the end; (ii) at the second end of each second leading stage and each second posterior Page 41 508265 VI. The scope of the patent application leaves an open fluid connection between the first ends of the subsequent stages. The fluid connection is suitable for facilitating inter-stage flow, and is generally parallel to the outer periphery of the module; and (b) each second leading stage The surface area of the diaphragm is 1 to 2.5 times the surface area of the diaphragm immediately after the second subsequent stage, and the surface area of the second stage decreases from the first stage to the last stage. -4 · If the module of the scope of patent application No. 3, where the valve is a one-way valve, its opening direction makes the group of scope of patent application No. 1 and the scope of patent application: The regrouping of No. 3 can use the flow Menstrual fluid effector. _ 5. If the module of the scope of patent application is No. 1, the membrane is reverse osmosis-or nanofiltration membrane. 6. For the module of the first scope of patent application, the first section has a circular cross section, and the stage is in the shape of a cylindrical fan segment. 7. If the module in the scope of patent application is the first one, each head is composed of a plurality of individual collars attached to each other, and the diaphragm is installed in the opposite paired collar area containing the collars of each head. 8. For the module of the seventh scope of the patent application, the first part has a cylindrical section, and the collar is in the shape of a cylindrical sector. 9. For the module in the scope of patent application item 8, all the collars are the same size and shape. 10. The module according to item 8 of the scope of patent application, in which each of the diaphragms installed in the collar does not exceed about 35 mm from the edge of the diaphragm bundle installed in the collar. 11. The module according to item 7 of the patent application, wherein the membrane is a reverse osmosis membrane or a nanofiltration membrane. 1 2. —A method for manufacturing the seventh module of the scope of patent application, including steps Page 42 508265 6. The scope of patent application is as follows: (a) Provide multiple collars of the same size and shape, and have a sufficient number of multiple collars to form a pair of heads; (b) Install the diaphragm into opposite pairs of shafts Inside the ring; (c) perform any required diaphragm coating or testing steps on the individual opposing pairs of collars; (d) glue the opposing pairs of collars together to form a pair of opposing headers; (e) apply The head is attached to the end cap as the end; and (f) the end cap is attached. 1 3. The method according to item 12 of the patent application scope, in which the diaphragm is simultaneously loaded into all the opposite pairs of collars, and the collar is kept in the installation mold, and any required diaphragm coating or testing is performed. Before the steps, the opposing pairs of collars are separated from each other. 1 4. A filter module comprising: (a)-opposite heads; (b) a plurality of hollow fiber membranes, which are installed in the head so that the inner cavity of the membrane is opened to the distal surface of the head; (c) a shell between the heads It extends with permeate outlet to define the permeate collection chamber. The permeate collection chamber is in fluid communication with the outside of the diaphragm; (d) — Caps or caps are fitted on the heads, and the caps surround the heads. Peripheral surface (e) module feed inlet, so that the feed water flows into the diaphragm cavity; _ (f) module exit, so that retentate flows out of the diaphragm cavity from the module 508265 6. Application scope of patents A plurality of individual collars are attached to each other, and the diaphragm is inserted into an opposing pair of collars containing each of the first collars. 1 5. If the module of the scope of patent application No. 14 is used, the first section has a cylindrical section, and the collar is in the shape of a cylindrical sector. 1 6. If the module of the scope of patent application No. 15 is used, all the collars are the same size and shape. 1 7. The module according to item 15 of the scope of patent application, in which the collar includes a chord length not exceeding 3 inches. _ 1 8. If the module of the scope of patent application No. 14 is used, the membrane is reverse osmosis, or nanofiltration membrane. 1 9. A method of manufacturing a module in the 14th patent application scope, comprising the steps of: (a) providing multiple collars of the same size and shape, and making a sufficient number of multiple collars to form a pair of headers; (b) Put the diaphragm into the opposite paired collars; (c) Apply any required diaphragm coating or test steps to the individually opposed paired collars; (d) glue the opposite paired collars together, Forming pairs of opposite heads—heads; (e) attaching the head to the end cap as the end; and (f) those with end caps. 20. The method according to item 19 of the scope of patent application, wherein the diaphragm is simultaneously loaded into _ all opposite pairs of collars, and the collars are kept in the installation mold, and any required diaphragm coating or testing steps are performed. Before, the opposite paired collars Page 508 508265 6. The scope of patent application is separated from each other. 2 1-a method of filtering water to remove hardness, including + (a) let the water to be filtered flow into the hollow v flowing from the inside is: inside the first end, enough Selective rejection of the hardness-enhancing diaphragm module (b) Collecting softened permeate from the outer surface of the diaphragm; welcome ('c) Collecting retentate from the second end of the module; and-(d) Reversing the feed stream regularly Through the direction of the module, make 1 flow into the second end of the module, and the retentate will pass through the water from the first to the first module of the module. 22 · If the method of the scope of patent application for item 21, it is = outflow. _ The module of the profit scope item 3. 'Group is an application-specific 2 3 · — a filtering method to remove hardness, including step 骒 (a) to provide the module of the scope of patent application No. 1 ... 75%, the initial permeability is greater than 0. igfd / psi; X refuse At least _ (b) feed the feed water into the feed inlet of the module through the module; single flow of feed water (c) extract retentate from the module outlet; and (d) extract permeate from the permeate outlet The lowest feed / retentate of 0.15 and 0.6 f t / s at any stage. Thousands; about 24. The method of claim 23 of the patent scope, wherein the lowest feed / retentate rate at any stage is between about 0.2 and 0.3 ft / s. 2 5 · —A method of filtering water to remove hardness, including the following steps: (a) The water to be filtered flows against the feed or retentate side of the hollow fiber membrane module. The feed or retentate of the diaphragm Side is its internal cavity, diaphragm is suitable for selection Page 45 508265 Sixth, the scope of patent application selective rejection caused by hardness; (b) collect softened permeate from the permeate side of the diaphragm; (c) collect retentate from the module; and (d) in the feed water Before entering the hollow fiber membrane cavity, add carbon dioxide to the feed water. 2 6 · If the method of the scope of patent application No. 25, where carbon dioxide is continuously added to the feed water, the amount of which makes the Langelier index zero or slightly negative 0 2 7 · If the method of the scope of patent application No. 25, Among them, when the demand for permeate is low, carbon dioxide is always added to the feed water, instead of adding two When carbon dioxide is not oxidized, the permeate produced when carbon dioxide is added is discarded. , 28. If the method in the scope of application for the patent No. 25, it also includes periodically reversing the direction of the feed t and the module, and adding carbon dioxide to the water, and the water to be filtered flows into the module. p Taixin, for example, the method of applying for patent No. 21 in the Fanyuan Garden, also includes adding water to the water to be filtered, and the flow to the filter is reversed into the module. Degrees, including #nano osmosis, or reverse osmosis device 'suitable for removing hard and attractive ^ g 2 2 filter or reverse osmosis osmosis module from the feed water, enough to reject the hardness, and the module out of the mold Group feed inlet, remove the retentate containing hardness (b) I material and the permeate outlet after removing the permeate after the treatment = the inlet of the module that feeds the pressure to the filter module and the fluid feed to the filter module. Page 46 508265 6. Application patent scope Luxury patent scope ----- 1 Controlled carbon dioxide addition is continued & sprayed into the pressurized feed water to include, and have at least one outlet to In addition to oxidizing fluid u carbon oxide pathway, fluid connection & -3Γ: ΐ = or nanometer pass through die 4 (=) permeate pathway, fluid connection includes: (b) pressurized diaphragm slot for permeate outlet And inlet 32 ':: connected to the permeate path i, = ^ :; permeate, a device with a tank tap water supply pressurizer 9, where the feed f ^ 3 is used, as in the scope of the patent application No. 3 丨 34 = :: ί as described in item 1 of the scope. The following penetrations were used: ^ * (W to make the pressurized water to be filtered two = rejection hardness; feed / retentate (0 collected tritium permeate from the wedge side, · Erzhen group collected retentate , And (the acupoint phase stops permeating; and pushing ιι 丨 1 & acidic or feed that will open the silk in the water (1 retentate side will open / acidic fluid, threatening to shoot eight molds) Group formation of acid (1 ^ = module feed / retentate side with holding acid # + slave "body, after a selected period of time and keeping 駄 I · raw or carbon dioxide will be added in the water side scare page 47 508265 6. Scope of patent application (iii) After the selected time has elapsed, the acidic or acidic fluid in the water will be flushed out from the feed / retentate side of the module. 3 5 • If the patent application park No. 34 Method, in which the acidic or acidic fluid in water is sprayed into the feed / retentate side of the module for a period of time, which is sufficient to exclude the feed / retentate on the module's feed / retentate side 3 6. The method according to item 35 of the scope of patent application, wherein the fluid is acidic, and p Η is between 4.5 and 6.5. 3 7. According to the scope of patent application 36. The method according to item 6, in which the selected time is between 20 and 30 minutes. 3 8. — A filtering method, including the steps of: using the following penetration: (a) the pressurized water to be filtered flows into the membrane module The feed / retentate side is sufficient to selectively reject hardness; (b) collect softened permeate from the permeate side of the module; (c) collect retentate from the module; and (d) stop infiltration periodically; and (i) ) Spraying the gas that will form acid in the water into the feed / retentate side of the module, after a period of time, it is enough to substantially exclude the feed / retentate on the feed / retentate side of the module; ( ii) Keeping the gas on the feed / retentate side of the module in water will form an acid gas, after a selected time; and Hexin (iii) after the selected time, remove the acidic or acidic fluid in water from the mold, The group of feed / retentate side punch. Page 48 508265 VI. Scope of patent application 3 9. The method according to item 38 of the scope of patent application, in which the gas that will form an acid in water is carbon dioxide gas. 40. The method according to item 39 of the scope of patent application, wherein the selected time is between 20 and 30 minutes. 41. The method of claim 40, wherein the carbon dioxide gas is maintained in the inner cavity of the hollow fiber membrane at a pressure between 5 and 5 Ops i for a selected period of time. 4 2. The method according to item 40 of the patent application, wherein carbon dioxide forms an acid in water in the cell pores of the membrane, and the pH is between 4.5 and 6. _ Page 49