Membrane-Based Liquid Filtration Installation and Method for Producing Drinking Water Therewith Without Post-Mineralisation

Abstract

Installation for the pressurised filtration of liquid with a view to producing drinking water, comprising at least one membrane-based drinking-water production unit (MPU), each MPU comprising: a plurality of filtration blocks each containing a bundle of pressure tubes mounted in parallel, each pressure tube accommodating at least two membrane-based filtration modules with spiral membranes or hollow-fibre membranes mounted in series, means (20) for feeding the liquid that is to be filtered, means for removing the filtered liquid, and means (30) for removing the concentrate, characterised in that the membranes of the filtration modules are of at least two different types selected from the group consisting of reverse-osmosis membranes and low-pressure reverse-osmosis membranes (4-6), on the one hand, and nanofiltration membranes (1-3) on the other hand, and in that at least one MPU comprises means (21-26) making it possible to alter the order in which the blocks of pressure tubes that it groups together are supplied with fluid. The method consists in supplying the filtration blocks of at least one MPU in a first order of supply in which the tubes containing nanofiltration membranes are at the head of the MPU and then in supplying the pressure tubes in a second order of supply in which the pressure tubes containing reverse-osmosis membranes or low-pressure reverse-osmosis membranes are at the head of the MPU.

Claims

1-14. (canceled)

15. Installation for the pressurised filtration of liquid with a view to producing drinking water comprising at least one membrane-based drinking-water production unit (MPU), each MPU comprising: a plurality of filtration blocks each containing a bundle of pressure tubes mounted in parallel, each pressure tube accommodating at least two membrane-based filtration modules with spiral membranes or hollow-fibre membranes mounted in series, means for feeding the liquid that is to be filtered, means for removing the filtered liquid, and means for removing the concentrate, characterised in that said membranes of said filtration modules of said installation are of at least two different types selected from the group consisting of reverse-osmosis membranes and low-pressure reverse-osmosis membranes on the one hand, and nanofiltration membranes on the other hand, and in that said at least one MPU comprises means making it possible to alter the order in which the blocks of pressure tubes that it groups together are supplied.

16. Installation according to claim 15 characterised in that said membranes of at least two different types are provided in different pressure tubes.

17. Installation according to claim 15 characterised in that said membranes of at least two different types are provided in the same pressure tubes.

18. Installation according to claim 15 characterised in that said nanofiltration membranes allow a rejection rate less than or equal to 70% of the calcium during a standard test with CaCl.sub.2.

19. Installation according to claim 15 characterised in that said reverse-osmosis membranes and/or said low-pressure reverse-osmosis membranes allow a rejection rate greater than 90% of the calcium during a standard test with CaCl.sub.2.

20. Installation according to claim 15 characterised in that it has a ratio of the numbers of nanofiltration membranes over the total number of membranes comprised between 5% and 95%.

21. Installation according to claim 15 characterised in that said nanofiltration membranes have a permeability greater than 3 L/h/m.sup.2/bar and allow a rejection rate of the monovalent salts less than 82%, according to the “standard NaCl test”.

22. Installation according to claim 15 characterised in that said low-pressure reverse-osmosis membranes have a permeability greater than 3 L/h/m.sup.2/bar and allow a rejection rate of the monovalent salts greater than or equal to 82%, according to the “standard NaCl test”.

23. Installation according to claim 15 characterised in that said reverse-osmosis membranes have a permeability greater than 3 L/h/m.sup.2/bar and allow a rejection rate of the monovalent salts greater than or equal to 82%, according to the “standard NaCl test”.

24. Method for filtering liquid for the production of drinking water implementing an installation according to claim 15 characterised in that it comprises the steps of supplying the filtration blocks of at least one MPU in a first order of supply wherein the tubes containing nanofiltration membranes are at the head of the MPU, then, according to the variation in a parameter, supplying the pressure tubes in a second order of supply wherein the pressure tubes containing reverse-osmosis membranes or low-pressure reverse-osmosis membranes are at the head of the MPU.

25. Method according to claim 24 characterised in that each MPU is organised in filtration stages connected in series, each filtration stage comprising, according to the possible configurations thanks to the implementation of said means making it possible to alter the order of supply of said blocks of pressure tubes, either a single filtration block, or 2 or more filtration blocks mounted in parallel.

26. Method according to claim 25 implemented with an installation comprising a plurality N of MPUs, with N>1 an integer, characterised in that it comprises a step of supplying the blocks of x/N MPUs, with x an integer varying from 0 to N, according to said first order, and the blocks of the remaining MPUs according to said second order, and varying x in such a way that the filtered water obtained at the outlet of the installation meets a quality factor.

27. Method according to claim 24 characterised in that said parameter is selected from the group consisting of the temperature of the water to be treated and the calcium concentration of the liquid to be treated.

28. Method according to claim 24 characterised in that said quality factor is the hardness of said filtered water obtained at the outlet of the installation.

29. A process of treating water and producing drinking water in a system including at least one membrane-based drinking water production unit (MPU) where the MPU includes a plurality of filtration blocks with each block containing a bundle of pressure tubes with each pressure tube including at least two membrane-based filtration modules; wherein the filtration blocks are divided into at least first and second groups with the pressure tubes of the first group of filtration blocks containing nanofiltration membranes, and wherein the pressure tubes of the second group of filtration blocks contains reverse osmosis membranes; wherein the MPU includes a piping network connecting the filtration blocks and wherein the piping network includes a first group of valves and a second group of valves; and wherein the process comprises: opening the first group of valves and closing the second group of valves; in a first stage of the process with the first group of valves being open and the second group of valves being closed, directing the water to be treated into the piping network and into one or more of said first group of filtration blocks containing nanofiltration membranes, and thereafter directing the water into one or more of said second group of filtration blocks containing reverse osmosis membranes; during the first stage, the filtration blocks of the first and second groups produce a permeate and a concentrate, both of which are directed from the piping network; closing the first group of valves and opening the second group of valves; in a second stage of the process where the second group of valves are open and the first group of valves are closed, directing the water to be treated into the piping network and through one or more of said second group of filtration blocks containing the reverse osmosis membranes, and thereafter directing the water into the one or more of the first group of filtration modules containing the nanofiltration membranes; during the second stage, the first and second groups of filtration blocks produce permeate and the concentrate, both of which are directed from the piping network; and wherein during the first stage of the process, the nanofiltration membranes function at the head of the process and the reverse osmosis membranes function at the tail of the process, and wherein during the second stage of the process, the reverse osmosis membranes function at the head of the process and the nanofiltration membranes function at the tail of the process.

30. The process of claim 29 wherein the reverse osmosis membranes include low pressure reverse osmosis membranes.

Description

LIST OF FIGURES

[0035] The invention, as well as the different advantages that it has will be easier to understand thanks to the following description of embodiments of the latter given for the purposes of information and in a non-limiting way, in reference to the drawings wherein:

[0036] FIG. 1 schematically shows a first embodiment of an installation according to the present invention, the direction of the liquids transiting therein being indicated by arrows corresponds to a first operating configuration referred to as “high temperature configuration”.

[0037] FIG. 2 schematically shows the same installation operating according to a second configuration referred to as “low water temperature configuration”.

[0038] FIG. 3 schematically shows a second embodiment of an installation according to the present invention, with the direction of the liquids transiting therein being indicated by arrows corresponds to a first operating configuration referred to as “high temperature configuration”.

[0039] FIG. 4 schematically shows the same installation as that shown in FIG. 3 operating according to a second configuration referred to as “low water temperature configuration”.

DESCRIPTION OF EMBODIMENTS

[0040] A first embodiment of an installation according to the present invention is comprised of six identical MPUs (N=6), each one being sized to produce 695 m.sup.3/h of drinking water with a yield of 85% from water having an osmotic pressure less than 20 bars.

[0041] One of these MPUs is shown in FIGS. 1 and 2. It comprises, in addition to means 20 for feeding the liquid that is to be filtered and means for removing 30 rejected liquid or concentrate, six filtration blocks 1 to 6. Each filtration block contains thirty pressure tubes. Each pressure tube contains six membrane-based filtration modules mounted in series. Thus this MPU contains 1080 membrane-based filtration modules. Therefore the plant, which contains six MPUs, each one with 1080 membranes, includes a total of 6480 membranes.

[0042] More precisely, three of these blocks contain NF modules and the other three LPRO modules. In the framework of this embodiment, the NF membranes are spiral membranes marketed under commercial reference DOW FILMTEC NF270-400 and LPRO membranes are spiral membranes marketed under commercial reference DOW FILMTEC ECO-400.

[0043] The NF membranes used have a flow rate of 55.6 m.sup.3/day under standard CaCl.sub.2 test and a rate of rejection in calcium of 40 to 60% under standard CaCl.sub.2 test.

[0044] The LPRO membranes used have a flow rate of 44 m.sup.3/day under standard NaCl test and make it possible to reject 99.7% of the monovalent ions.

[0045] In FIGS. 1 and 2 the blocks 1, 2 and 3 with NF modules and the blocks 4, 5 and 6 with LPRO modules are therefore distinguished.

[0046] According to the invention, each UMP of the installation is provided with means making it possible to alter the order in which the blocks of pressure tubes that it groups together are supplied. These means are comprised of valves, or of any other isolation device, 21 to 26.

[0047] According to the invention, the order in which the modules of each UMP are supplied can vary according to a parameter.

[0048] Thus, in reference to FIG. 1, according to a first configuration, the valves or isolation device 21, 23 and 26 are open while the valves or isolation devices 22, 24 and 25 are closed. A first filtration stage comprised of NF blocks 1, 2 and 3 supplied in parallel, a second filtration stage comprised of LPRO blocks 4, 5 supplied in parallel, and a third filtration stage comprised of the LPRO module block 6, are as such delimited.

[0049] According to such a configuration, the LPRO takes place at the tail of MPU over two stages, which allows for a good rejection of the micropollutants and of the calcium without degrading the operating pressure.

[0050] According to the invention, the order of supply of the blocks 1 to 6 can be altered by closing the valves or isolation devices 21, 23 and 26 and by opening the valves or isolation devices 22, 24 and 25. According to this second configuration, the first filtration stage is comprised of the LPRO blocks of modules 4, 5, 6 mounted in parallel, the second filtration stage is comprised of NF blocks of modules 2 and 3 and the third filtration stage is comprised of the NF block of modules 1.

[0051] According to such a second configuration, the nanofiltration takes place at the tail of the MPU over two stages, thus favouring a drop in pressure while still offering a good rejection of micropollutants.

[0052] Thus, the block 1 operating in parallel in the first configuration operates in series in the second configuration and the block 6 operating in series in the first configuration operates in parallel in the second configuration.

[0053] Simulations were carried out to show that, thanks to the invention, the hardness of the water produced by the installation in a fixed interval can be maintained, for example between 8 and 9° F., while still maintaining good rejection of micropollutants, even in the case of a variation in the temperature or in the quality of the water to be filtered.

[0054] In a first battery of simulations, the installation was calculated to filter water with a constant hardness and with a temperature that varies according to the seasons, having the following characteristics:

[0055] Calcium content=110 mg/l,

[0056] Magnesium content=8 mg/l,

[0057] Sodium content=22 mg/l,

[0058] Bicarbonate content=230 mg/l, nitrates=20 mg/l,

[0059] Chloride content=30 mg/l,

[0060] Sulphate content=120 mg/l,

[0061] SiO.sub.2 content=10 mg/l,

[0062] pH=7.1

[0063] and of which the temperature varied over one year by 5° C. to 25° C.

[0064] The treated water flow rate produced is 100,000 m.sup.3/d. The objective for the water produced is set to a minimum of 30 mg/l of calcium (corresponds to a hardness of 8° F.) regardless of the temperature of the water to be filtered. The maximum concentration sought is 35 mg/l of calcium (corresponds to a hardness of 9° F.). In the framework of this first battery of simulations the proportion (x/6) of MPU of the installation operating in the first configuration and the MPU operating in the second configuration are varied according to the temperature of the water to be filtered.

[0065] Table 1 hereinafter indicates for each temperature window, and for each proportion (0/6; 1/6; 2/6; 3/6; 4/6; 5/6; 6/6), the calcium concentration (Ca, major constituent of the hardness) of the permeate, the nitrate (NO.sub.3) concentration of the permeate as well as the supply pressure (P) of the MPUs.

TABLE-US-00001 TABLE 1 Temperature 5° C. Temperature 10° C. Temperature 15° C. Temperature 20° C. Temperature 25° C. Ca P NO.sub.3 Ca P NO.sub.3 Ca P NO.sub.3 Ca P NO.sub.3 Ca P NO.sub.3 (mg/l) (bar) (mg/l) (mg/l) (bar) (mg/l) (mg/l) (bar) (mg/l) (mg/l) (bar) (mg/l) (mg/l) (bar) (mg/l) 0/6 30.9 7.9 15.7 35.9 6.4 16.5 40.6 5.3 17 45.1 4.3 17.6 48.9 3.7 17.8 1/6 28.3 8.1 14.7 33 6.6 15.5 37.4 5.6 16 41.7 4.6 16.6 45.4 4 16.9 2/6 25.6 8.2 13.7 30 6.8 14.5 34.2 5.8 15 38.3 4.8 15.6 41.9 4.2 16 3/6 23 8.4 12.7 27.1 7.1 13.5 31 6 14.1 34.9 5.1 14.6 38.4 4.4 15 4/6 20.4 8.5 11.6 24.2 7.3 12.5 27.8 6.3 13.1 31.4 5.3 13.7 34.8 4.7 14.1 5/6 17.8 8.7 10.6 21.2 7.5 11.5 24.6 6.5 12.1 28 5.6 12.7 31.3 4.9 13.2 6/6 15.1 8.8 9.6 18.3 7.7 10.5 21.4 6.8 11.1 24.6 5.8 11.7 27.8 5.2 12.3

[0066] In comparison, the same water was treated with an installation of the double branch type of the prior art implementing eight MPUs each containing 135 pressure tubes arranged in three stages. Each pressure tube containing six modules of membrane-based filtration, this installation therefore contains the same number of membrane-based filtration modules as that according to the invention, which is 6480 modules. The same NF and LPRO modules as in the installation according to the invention were implemented.

[0067] In order to allow for the obtaining in winter, at a temperature comprised between 5° C. and 10° C., with a minimum hardness of the water produced corresponding to a content of at least 30 mg/l of calcium, the double-branch installation contains a proportion of 25% of NF modules and 75% of LPRO modules.

[0068] This double branch was used to filter the same water with the same variations in temperatures. The table 2 hereinafter indicates for each temperature window, the concentrations in calcium (major constituent of the hardness), in nitrates and the supply pressure.

TABLE-US-00002 TABLE 2 Temperature 5° C. Temperature 10° C. Temperature 15° C. Temperature 20° C. Temperature 25° C. Ca P NO.sub.3 Ca P NO.sub.3 Ca P NO.sub.3 Ca P NO.sub.3 Ca P NO.sub.3 (mg/l) (bar) (mg/l) (mg/l) (bar) (mg/l) (mg/l) (bar) (mg/l) (mg/l) (bar) (mg/l) (mg/l) (bar) (mg/l) 30.4 6.5 14.4 35 5.6 14.9 39.4 4.9 15.4 43.2 4.5 15.8 46.6 4.2 16.1

[0069] As can be seen in table 1, it was possible to maintain the calcium concentration of the water produced by the installation between 30 mg/l and 35 mg/l by varying the proportion (MPU operating in the first configuration/total MPU) therefore by altering the order of supply of the blocks of pressure tubes of the MPUs. The invention thus makes it possible to maintain the calcium content of the treated water at about 30 mg/L. Such a result was not able to be obtained with the double branch of the prior art, as shown by the results in table 2 which show an increase in the calcium content well above the desired limit of 35 mg/l in practice having ranged up to 46 mg/l.

[0070] These simulations also make it possible to demonstrate that the invention makes it possible to obtain better reduction rate in the nitrates.

[0071] It is demonstrated via tests on 5 membranes of different natures that the rejection of nitrates is a good indicator of the rejection of micropollutants. The results of these tests are mentioned in table 3 hereinafter. Thus, the configurations allowing for a good rejection of nitrates, including at the highest temperatures, are to be favoured when a better rejection of micropollutants is sought.

TABLE-US-00003 TABLE 3 Diuron rejection Nitrate rejection (herbicide) <1% <1% 58% 54% 75% 88% 81% 91% 95% 98%

[0072] In a second battery of simulations, the installation was calculated to filter water at a constant temperature and of a variable hardness having the following characteristics:

[0073] Magnesium content=8 mg/l,

[0074] Sodium content=22 mg/l,

[0075] Bicarbonate content=230 mg/l, nitrates=20 mg/l,

[0076] Chloride content=30 mg/l,

[0077] Sulphate content=120 mg/l,

[0078] SiO.sub.2 content=10 mg/l,

[0079] Temperature=15° C.

[0080] pH=7.1

[0081] and of which the calcium content varied from 90 to 140 mg/l.

[0082] The treated water flow rate produced is 100,000 m3/d. The objective for the water produced is set to a minimum of 30 mg/l of calcium regardless of the calcium concentration of the inlet water to be filtered. The maximum concentration sought is 35 mg/l of calcium.

[0083] In the framework of this second battery of simulations, the proportion (x/6) of MPU of the installation operating in the first configuration and of MPU operating in the second configuration are varied according to the calcium content of the water to be filtered.

[0084] Table 4 hereinafter indicates for each calcium content in the inlet water to be filtered, and for each proportion (0/6; 1/6; 2/6; 3/6; 4/6; 5/6; 6/6), the calcium concentration (major constituent of the hardness) of the permeate, the nitrate concentration of the permeate and the supply pressure.

TABLE-US-00004 TABLE 4 90 mg/l of Ca in 110 mg/l of Ca in 130 mg/l of Ca in 140 mg/l of Ca in inlet water inlet water inlet water inlet water Ca NO.sub.3 P Ca NO.sub.3 P Ca NO.sub.3 P Ca NO.sub.3 P (mg/l) (mg/l) (bar) (mg/l) (mg/l) (bar) (mg/l) (mg/l) (bar) (mg/l) (mg/l) (bar) 0/6 33.2 13.91 5.24 40.6 17.01 5.31 48 20.12 5.38 51.8 21.66 5.42 1/6 30.6 13.1 5.5 37.4 16 5.6 44.3 19 5.6 47.8 20.5 5.7 2/6 27.9 12.3 5.7 34.2 15 5.8 40.6 17.8 5.9 43.7 19.2 5.9 3/6 25.3 11.4 6 31 14.1 6 36.8 16.7 6.1 39.7 18 6.1 4/6 22.6 10.6 6.2 27.8 13.1 6.3 33.1 15.6 6.3 35.7 16.8 6.4 5/6 20 9.8 6.5 24.6 12.1 6.5 29.3 14.4 6.6 31.7 15.6 6.6 6/6 17.3 9.0 6.7 21.4 11.1 6.8 25.6 13.3 6.8 27.7 14.4 6.9

[0085] In comparison, the same water was treated with an installation of the double branch type of the prior art implementing eight MPUs each containing 135 pressure tubes arranged in three stages. Each pressure tube containing six membrane-based filtration modules, this installation therefore contains the same number of membrane-based filtration modules as that according to the invention, which is 6480 modules. The same modules NF and LPRO as in the installation according to the invention were implemented.

[0086] In order to be able to ensure a minimum hardness of the water produced corresponding to a content of at least 30 mg/l of calcium, for a supply water containing 90 mg/l of calcium, the double-branch installation contains a proportion of 30% of NF modules and 70% of LPRO modules.

[0087] This double branch was used to filter the same water with the same variations in concentrations in calcium. Table 5 hereinafter indicates for each calcium content in the inlet water, the concentrations in calcium (major constituent of the hardness) and in nitrates in the permeate and the supply pressure.

TABLE-US-00005 TABLE 5 90 mg/l of Ca in 110 mg/l of Ca in 130 mg/l of Ca in 140 mg/l of Ca in inlet water inlet water inlet water inlet water Ca NO.sub.3 P Ca NO.sub.3 P Ca NO.sub.3 P Ca NO.sub.3 P (mg/l) (mg/l) (bar) (mg/l) (mg/l) (bar) (mg/l) (mg/l) (bar) (mg/l) (mg/l) (bar) 30.1 11.79 4.93 36.84 14.44 4.96 43.57 17.1 5.04 47.02 18.44 5.26

[0088] This second battery of simulations makes it possible to demonstrate that the prior art leads to a calcium content of the water produced ranging from 30 to 47 mg/l while the invention makes it possible to maintain this concentration around 30-35 mg/l.

[0089] The reduction in nitrates, and therefore of the micropollutants is moreover better thanks to the invention, in most cases.

[0090] A second embodiment of an installation according to the present invention comprises six MPUs such as shown in FIGS. 3 and 4 similar to the one shown in reference to FIGS. 1 and 2 except in that it has additional valves or other isolation device (21a, 22a, 22b, 22c, 23a, 23b) and in that it comprises four filtration blocks instead of six. More precisely, one of these blocks (block 1) contains thirty pressure tubes, each pressure tube containing six modules NF, another block (block 2a) contains sixty pressure tubes, each pressure tube containing six NF modules, another block (block 4) contains thirty pressure tubes, each pressure tube containing six LPRO modules and another block (block 6a) contains sixty pressure tubes, each pressure tube containing six LPRO modules. The capacity of the MPU shown in these FIGS. 3 and 4 is therefore the same as that shown in FIGS. 1 and 2.

[0091] In reference to FIG. 3, according to a first configuration, the valves or isolation device 21, 21a, 23, 23a, 23b and 26 are open while the valves or isolation devices 22, 22a, 22b, 22c, 24 and 25 are closed. A first filtration stage comprised of the two NF blocks 1 and 2a supplied in parallel, a second filtration stage comprised of the LPRO block 6a, and a third filtration stage comprised of the LPRO block 4, are thus delimited.

[0092] According to such a configuration, the LPRO takes place at the tail of the MPU over two stages, which allows for good rejection of micropollutants and of calcium without degrading the operating pressure.

[0093] According to the invention, the order in which the blocks are supplied can be altered by closing the valves or isolation devices 21, 21 a, 23, 23a, 23b and 26 and by opening the valves or isolation devices 22, 22a, 22b, 22c, 24 and 25.

[0094] According to this second configuration, the first filtration stage is comprised of the LPRO blocks of modules 4 and 6a mounted in parallel, the second filtration stage is comprised of the NF block 2a and the third filtration stage is comprised of the NF block of modules 1.

[0095] According to such a second configuration, the nanofiltration takes place at the tail of the MPU over two stages, thus favouring a drop in pressure while still offering a good rejection of micropollutants.

[0096] Thus, the block 1 operating in parallel in the first configuration operates in series in the second configuration and the block 6a operating in series in the first configuration operate in parallel in the second configuration.