Abstract:
A method and system for treating water in order to desalinate the water where the system and method includes a reverse osmosis or distillation unit for producing a first concentrate and at least partially desalinated water. The first concentrate stream is directed to a first demineralization unit which utilizes nanofiltration membranes to treat the first concentrate stream so as to produce a permeate and a second concentrate stream. The second concentrate stream is directed to a second demineralization unit that includes an ion exchange device which in turn treats the second concentrate stream by producing a stream of at least partially demineralized water and third concentrate stream. The stream of at least partially demineralized water is mixed with the stream of at least partially desalinated water produced by the reverse osmosis or distillation unit.

Description:
This application is a U.S. National Stage Application of PCT Application No. PCT/EP2010/057801, with an international filing date of 3 Jun. 2010. Applicant claims priority based on French Patent Application No. 0953700 filed 4 Jun. 2009. The subject matter of these applications is incorporated herein. 
     FIELD OF THE INVENTION 
     The field of the invention is that of water treatment. More specifically, the invention relates to the treatment of water, in particular seawater or brackish water, for desalination of same. 
     PRIOR ART 
     Desalination of seawater is a practice commonly implemented in order to reduce the concentration of various salts dissolved in the water. To this end, it is known to filter salt-rich water through reverse osmosis membranes. This type of filtration by reverse osmosis can be applied to any type of water containing salts such as seawater or brackish water. 
     This type of treatment by reverse osmosis is particularly effective in that it enables purified water (or permeate), with a considerably reduced salt concentration, to be produced. This is shown clearly in the columns of table 1, which shows the results of the treatment of seawater by reverse osmosis with a conversion rate equal to 52.8%. It is noted that the conversion rate is equal to the ratio of the flow rate of the treated water produced over the flow rate of water to be treated. 
     
       
         
               
             
               
               
               
               
               
             
               
               
               
               
               
             
           
               
                 TABLE 1 
               
             
             
               
                   
               
               
                 results of the treatment of seawater by 
               
               
                 reverse osmosis with a conversion rate of 52.8%. 
               
             
          
           
               
                   
                   
                   
                 Desalinated 
                   
               
               
                   
                   
                   
                 water 
               
               
                   
                   
                   
                 (reverse 
               
               
                   
                 Parameters 
                 Seawater 
                 osmosis) 
                 Concentrate 
               
               
                   
                   
               
             
          
           
               
                   
                 Cations 
                   
                   
                   
               
               
                   
                 (mg/l) 
               
               
                   
                 Ca 2+   
                 444.4 
                 0.15 
                 840.1 
               
               
                   
                 Mg 2+   
                 1382.7 
                 0.47 
                 2616.3 
               
               
                   
                 Ba 2+   
                 1.10 
                 0.1 
                 1.9 
               
               
                   
                 Na 2+   
                 12221.5 
                 19.6 
                 23056.6 
               
               
                   
                 K +   
                 416.1 
                 0.85 
                 784.3 
               
               
                   
                 Sr +   
                 4.94 
                 0.1 
                 9.34 
               
               
                   
                 Anions 
               
               
                   
                 (mg/l) 
               
               
                   
                 Cl −   
                 21754 
                 32.10 
                 41046.02 
               
               
                   
                 SO 4   2−   
                 2963.2 
                 0.40 
                 5610.26 
               
               
                   
                 HCO 3   −   
                 168.4 
                 0.38 
                 311.29 
               
               
                   
                 CO 3   2−   
                 3.5 
                 0.000 
                 9.49 
               
               
                   
                 NO 3   −   
                 1.0 
                 0.00 
                 1.87 
               
               
                   
                 Bore 
                 5.4 
                 0.35 
                 9.06 
               
               
                   
                 F −   
                 1.5 
                 0.02 
                 2.80 
               
               
                   
                   
               
             
          
         
       
     
     It may indeed be observed that the concentrations of the various salts initially present in the seawater are considerably reduced in the desalinated water obtained after treatment by reverse osmosis. The concentration of certain species in the desalinated water can reach values close to zero. 
     Another technique is commonly implemented in order to desalinate water. It involves distillation, and more specifically MSF-type (or Multi-Stage Flash) or MED-type (or Multi-Effect Distillation) distillation. 
     Such techniques of desalination by distillation are also particularly effective for reducing salts contained in the water to be treated. 
     However, desalination by reverse osmosis or by distillation, even if it is particularly effective, is not without disadvantages. 
     DISADVANTAGES OF THE PRIOR ART 
     In particular, desalination of water by reverse osmosis or by distillation is accompanied by the production and rejection of concentrates in the natural environment. 
     These concentrates have very high concentrations of salts initially present in the water to be treated. This is shown in the right-hand column of table 1 in which the concentrations of the different salts present in these concentrates are shown. It may in particular be observed that these concentrates are particularly rich in calcium and magnesium ions and bicarbonates. 
     In general, the concentration of organic and inorganic substances present in these concentrates is around 1.8 to 2 times higher than their initial concentration in the seawater. It is thus estimated that for a dissolved salt concentration in seawater on the order of 34 g/l, the salt concentration of the concentrate varies from 61 to 68 g/l. 
     Due to high salt concentrations of these concentrates, their rejection into the natural environment is not neutral, but may instead have a notable impact. 
     In particular, during desalination of seawater, these concentrates are rejected into the sea. This causes a sudden localized change in the salinity of the water. It has been observed that even if some animal or plant species are not affected by these sudden modifications of their environment, others are particularly sensitive to them. 
     The rejection of these concentrates into the natural environment therefore requires taking a certain number of precautions. In particular, various parameters such as ocean currents, meteorological conditions, and the type and/or abundance of certain animal or plant species, are taken into consideration in order to perform these rejections while limiting the impact thereof on the environment. 
     However, in certain areas in which such rejections are performed, irreversible effects on the lives, behavior and development of certain animal or plant species have been observed. 
     Another disadvantage of this desalination technique is related to the fact that concentrates it produces have an important volume as it contains a relatively important part of water. 
     The rejection into the natural environment of these concentrates has, in brief, two major disadvantages: 
     rejection into the natural environment of a large amount of inorganic and organic species initially present in the water to be treated; 
     loss in production of treated water. 
     OBJECTIVES OF THE INVENTION 
     The invention is intended in particular to overcome these disadvantages of the prior art. 
     More specifically, an objective of the invention is, in at least one embodiment, to provide a water desalination technique of which the implementation exerts only a limited impact on the environment, at least by comparison with the techniques of the prior art. 
     In particular, an objective of the invention is, in at least one embodiment, to provide such a technique that causes the amount of concentrate rejected into the natural environment to be reduced. 
     The invention also has the objective of enabling the implementation of such a technique that leads to the production of treated water in greater amounts than enabled by the techniques of the prior art. 
     Yet another objective of this invention is to provide, in at least one embodiment of the invention, such a technique that requires fewer maintenance actions, at least by comparison with the prior art techniques. 
     The invention is also intended to provide such a technique that is simple to implement and that is effective and economical. 
     DESCRIPTION OF THE INVENTION 
     These objectives, as well as others that will appear below, are achieved by a process for treating water for desalination of same, including a step of reverse osmosis or distillation of said water so as to produce water that is at least partially desalinated and a first concentrate. 
     According to the invention, such a process includes the following steps: 
     a first demineralization step, including a step of nanofiltration of said first concentrate so as to produce a permeate and a second concentrate; 
     a second step of demineralization of said second concentrate by means of at least one active material including cationic- and/or anionic-type ion exchange resins, said second demineralization step including the extraction of a third concentrate and the extraction of an at least partially demineralized water, said at least partially demineralized water being mixed with said at least partially desalinated water; 
     a step of regenerating said at least one active material, said regeneration step including a step of recirculation of said permeate. 
     Thus, the invention is based on an innovative approach to water desalination, which consists of demineralizing the first concentrate resulting from the water desalination by reverse osmosis or distillation, then demineralizing, by means of an active material, the second concentrate resulting from this first demineralization, so as to produce partially demineralized water and a third concentrate. 
     The demineralized water thus produced is mixed with the desalinated water resulting from the reverse osmosis or the distillation. This causes the volume of water produced to increase. 
     In addition, the demineralized water contains a certain number of species present in the second concentrate. The recycling thereof in the desalinated water eliminates rejection of the species that it contains into the natural environment. 
     The volume of residue resulting from the implementation of a process according to the invention is therefore considerably reduced. 
     Consequently, the impact of the rejection into the natural environment of concentrates resulting from the implementation of a process according to the invention is lower than that of the rejection of concentrates resulting from the implementation of processes according to the prior art. 
     Furthermore, the permeate resulting from the demineralization of the first concentrate is recirculated so as to enable the regeneration of the active material used for demineralization of the second concentrate. This enables the need for an external water supply in order to perform said regeneration to be avoided, and therefore the maintenance costs to be reduced. 
     The implementation of ion exchange resins enables the sulfates (SO 4   2− ) and other cations and anions present in the second concentrate to be retained effectively in order to produce at least partially demineralized water. 
     The implementation of a first demineralization step by nanofiltration enables a large part of the cations and anions initially present in the first concentrate to be effectively eliminated. 
     Preferably, said ion exchange resins are arranged in series or in mixed beds. 
     In this case, said nanofiltration step preferably implements membranes of which the cutoff is below 200 Daltons. 
     This enables a conversion rate of between 60 and 85% to be obtained. 
     A process according to the invention advantageously includes a step of evaluating the salt concentration of said first concentrate, a step of comparing said concentration with a reference value and a step of implementing said first demineralization step and/or said second demineralization step on the basis of said comparison. 
     This implementation enables one and/or the other of the first and second demineralization steps to be bypassed (or shunted) when the salt concentration of the first concentrate is low enough. 
     A process according to the invention includes a step of cooling said first concentrate. 
     In this case, said cooling step includes a step of circulating said first concentrate and said at least partially demineralized water in a heat exchanger. 
     The fact of cooling the first concentrate when its temperature becomes too high enables damage to the nanofiltration membranes implemented for the first demineralization to be prevented. 
     The technique discussed also relates to an installation for implementing a water treatment process according to the invention, said installation including a reverse osmosis or distillation unit. 
     According to the invention, such an installation includes: 
     first demineralization means, including membranes for nanofiltration of a first concentrate coming from said unit; 
     second demineralization means of a second concentrate coming from said first demineralization means, said second demineralization means including at least one active material including cationic- and/or anionic-type ion exchange resins; 
     supplying means of at least partially demineralized water coming from said second demineralization means in at least partially desalinated water coming from said unit; 
     regeneration means of said at least one active material, said regeneration means including means for recirculating a permeate coming from said first demineralization means to said second demineralization means. 
     Such an installation preferably includes a heat exchanger, said heat exchanger having a first inlet for said first concentrate, a second inlet for said at least partially demineralized water, a first outlet for the first concentrate connected to said first demineralization means, and a second outlet for said at least partially demineralized water leading into said at least partially desalinated water. 
     In this case, an installation according to the invention advantageously includes means for measuring the temperature of said first concentrate, means for comparing said temperature with a predetermined threshold value, means for routing said at least partially demineralized water to said exchanger, and means for controlling said means for routing on the basis of said comparison. 
     It is thus possible to cool the first concentrate when its temperature becomes too high so as to prevent damage to the nanofiltration membranes implemented for the first demineralization. 
    
    
     
       LIST OF FIGURES 
       Other features and advantages will appear more clearly in the following description of preferred embodiments, provided as simple illustrative and non-limiting examples, and the appended drawings, in which: 
         FIG. 1  shows a first embodiment of an installation according to the invention; 
         FIG. 2  shows a second embodiment of an installation according to the invention. 
     
    
    
     DESCRIPTION OF EMBODIMENTS OF THE INVENTION 
     1. Summary of the Principle of the Invention 
     The invention relates to the optimization of the desalination of water by reverse osmosis or distillation. 
     The general principle of the invention is based more precisely on the implementation, in such a process, of a first demineralization of the first concentrate coming from the desalination, of a second demineralization, by means of an active material, of the second concentrate coming from this first demineralization, and on the mixing of the demineralized water thus obtained with the desalinated water resulting from the desalination. 
     The implementation of a process according to the invention thus enables a larger volume of desalinated water to be produced. 
     It also enables, due to the fact that the demineralized water contains a certain amount of salts that were present in the concentrate resulting from the first demineralization, the rejection of said salts into the natural environment to be avoided. 
     In addition, this aspect of the invention makes it possible to help to reduce the volume of concentrate rejected into the natural environment. 
     The impact of the desalination by the implementation of a process according to the invention is therefore lower than that of the desalination techniques according to the prior art. 
     The general principle of the invention is also based on the recirculation of the permeate resulting from the first demineralization so as to regenerate the active material used for the second demineralization. 
     This enables the need for an external water supply in order to perform said regeneration to be avoided, and therefore the maintenance costs to be reduced. This also has an impact on the environment insofar as the water consumption for maintenance is reduced. 
     2. Example of a First Embodiment of the Invention 
     2.1 Installation 
     In reference to  FIG. 1 , a first embodiment of an installation for implementing a process according to the invention is presented. 
     As shown in said  FIG. 1 , such an installation includes a supply pipe for water to be treated  10 . This pipe  10  leads into a treatment or desalination unit  11 . 
     The treatment unit  11  can be a reverse osmosis unit including a plurality of membranes provided for this purpose. In an alternative, the unit  11  can include a distillation unit. More specifically, it may be a MED- or MSF-type distillation unit. This treatment unit  11  has a first outlet that is connected to a discharge pipe  12  for at least partially desalinated water. It has a second outlet that is connected to a pipe  13  for extracting a first concentrate. 
     The pipe  13  leads into a first demineralization unit  14 . 
     The demineralization unit  14  is a filtration unit. It advantageously integrates a plurality of nanofiltration membranes of which the cutoff is below 200 Daltons. This first demineralization unit  14  has a first outlet that is connected to a permeate discharge pipe  15 . It also has a second outlet that is connected to a second concentrate extraction pipe  16 . 
     The extraction pipe  16  leads into a second demineralization unit  17 . 
     The second demineralization unit  17  consists of a reactor housing ion exchange resins. These ion exchange resins can be cationic resins, anionic resins or mixed resins, i.e. comprised of a mixture of anionic resins and cationic resins. The choice of the type of resins implemented is dependent on the type of water treated and operating constraints. In addition, this second unit  17  has an inlet to which the discharge pipe  15  is connected. It also has a first outlet that is connected to a third concentrate extraction pipe  18 . It also has a second outlet that is connected to supply means including discharge pipe for at least partially demineralized water  19 . 
     The discharge pipe for at least partially demineralized water  19  leads into the discharge pipe  12  for at least partially desalinated water. 
     Such an installation also includes means for measuring the salt concentration of the first concentrate and means for comparing the value measured with a threshold value so as to bypass (or shunt) the implementation of one or the other of the first and second demineralization units when the salt concentration of the first concentrate is low enough. Secondary pipe networks (not shown) are provided for this purpose. 
     2.2 Process 
     A process for treating water by implementing an installation according to this first embodiment will now be described. 
     Such a water treatment process consists of routing the water to be treated into the desalination unit  11  by means of the pipe  10 . The water to be treated then undergoes reverse osmosis or distillation. 
     The implementation of such a reverse osmosis or distillation step leads to the production of 45 to 85% of at least partially desalinated water and 15 to 55% of a first concentrate rich in salts initially contained in the water to be treated. 
     The at least partially desalinated water is discharged from the desalination unit  11  by means of the discharge pipe  12 . The first concentrate is discharged from the desalination unit  11  by means of the extraction pipe  13 . 
     This concentrate is then routed in the direction of the first demineralization unit  14 . There, it undergoes a nanofiltration phase through membranes of which the cutoff threshold is preferably below 200 Daltons. 
     This step of nanofiltration of the first concentrate enables divalent cations or anions such as sulfates, calcium, magnesium, carbonates, and so on to be removed. The conversion rate of this nanofiltration step is advantageously between 60 and 85%. It is noted in this regard that the conversion rate is equal to the ratio between the flow rate of permeate produced and the flow rate of concentrate at the inlet of the first demineralization unit  14 . 
     The implementation of such a nanofiltration step leads to the production of 60 to 85% of a permeate containing monovalent cations and anions, such as chlorides, sodium, potassium, etc., and 15 to 40% of a second concentrate containing divalent cations and anions, such as sulfates, calcium, magnesium, carbonates, and so on. 
     The permeate is discharged from the first demineralization unit  14  by means of the discharge pipe  15 . The second concentrate is extracted from this demineralization unit  14  via the extraction pipe  16 . 
     This second concentrate is then routed to the inlet of the second demineralization unit  17 . There, it undergoes demineralization by being placed in contact with ion exchange resins. 
     This demineralization on ion exchange resins enables the sulfates and other divalent cations and anions present in the second concentrate to be retained. 
     The permeate coming from the first demineralization unit  14  is recirculated inside the second demineralization unit  17  via the pipe  15 . This recirculation enables a regeneration of the ion exchange resins to be implemented. 
     The implementation of this second demineralization step leads to the production of a third concentrate and at least partially demineralized water. 
     This third concentrate is extracted from the second demineralization unit  17  and rejected into the natural environment via the extraction pipe  18 . 
     The at least partially demineralized water is discharged from the second demineralization unit  17  via the discharge pipe  19 . This demineralized water is then mixed with the at least partially desalinated water circulating in the discharge pipe  12 . 
     The means for measuring the salt concentration of the first concentrate and means for comparing the value measured with a threshold value are implemented so as to bypass (or shunt) the implementation of one or the other of the first and second demineralization units when the salt concentration of the first concentrate is low enough. 
     3. Example of a Second Embodiment of the Invention 
     3.1 Installation 
     In reference to  FIG. 2 , a second embodiment of an installation for implementing a process according to the invention is presented. 
     As shown in said  FIG. 2 , such an installation includes a supply pipe for water to be treated  20 . This pipe  20  leads into a treatment or desalination unit  21 . 
     The treatment unit  21  can be a reverse osmosis unit including a plurality of membranes provided for this purpose. In an alternative, the unit  21  can include a distillation unit. More specifically, it may be a MED- or MSF-type distillation unit. This treatment unit  21  has a first outlet that is connected to a discharge pipe  22  for at least partially desalinated water. It has a second outlet that is connected to a pipe  23  for extracting a first concentrate. 
     The pipe  23  leads into a first inlet of a heat exchanger  24 . 
     The heat exchanger  24  is in this case a water/water exchanger. It has a first outlet that is connected to a pipe  25  leading into a first demineralization unit  26 . 
     The first demineralization unit  26  is a filtration unit. It advantageously integrates a plurality of nanofiltration membranes of which the cutoff is below 200 Daltons. This first demineralization unit  26  has a first outlet that is connected to a permeate discharge pipe  27 . It also has a second outlet that is connected to a second concentrate extraction pipe  28 . 
     The extraction pipe  28  leads into a second demineralization unit  29 . 
     The second demineralization unit  29  consists of a reactor housing ion exchange resins. These ion exchange resins can be cationic resins, anionic resins or mixed resins, i.e. comprised of a mixture of anionic resins and cationic resins. The choice of the type of resins implemented is dependent on the type of water treated and operating constraints. In addition, this second unit  29  has an inlet to which the discharge pipe  27  is connected. It also has a first outlet that is connected to a third concentrate extraction pipe  30 . It also has a second outlet that is connected to a discharge pipe for at least partially demineralized water  31 . 
     The discharge pipe for at least partially demineralized water  31  leads to a solenoid valve  35  to which supply means including two pipes  32  and  33  are connected. 
     The pipe  32  is connected to a second inlet of the exchanger  24 , which has a second outlet connected to a pipe  34  leading into the discharge pipe  22 . 
     The pipe  33  also leads into the discharge pipe  22 . 
     Control means, which are not shown in the figures, are connected to the solenoid valve  35  as well as to means for measuring the temperature of the first concentrate coming from the desalination unit  21 . 
     Such an installation also includes means for measuring the salt concentration of the first concentrate and means for comparing the value measured with a threshold value so as to bypass (or shunt) the implementation of one or the other of the first and second demineralization units when the salt concentration of the first concentrate is low enough. Secondary pipe networks (not shown) are provided for this purpose. 
     3.2 Process 
     A process for treating water by implementing an installation according to this second embodiment will now be described. 
     Such a water treatment process consists of routing the water to be treated into the desalination unit  21  by means of the pipe  20 . The water to be treated then undergoes reverse osmosis or distillation. 
     The implementation of such a reverse osmosis or distillation step leads to the production of 45 to 85% of at least partially desalinated water and 15 to 55% of a first concentrate rich in salts initially contained in the water to be treated. 
     The at least partially desalinated water is discharged from the desalination unit  21  by means of the discharge pipe  22 . The first concentrate is discharged from the desalination unit  21  by means of the extraction pipe  23 . 
     This concentrate is then routed in the direction of the inlet of the exchanger  24  inside of which its temperature is reduced. The concentrate is then discharged from the exchanger  24 , then routed to the inlet of the first demineralization unit  26  via the pipe  25 . There, it undergoes a nanofiltration phase through membranes of which the cutoff threshold is preferably below 200 Daltons. 
     This step of nanofiltration of the first concentrate enables divalent cations or anions such as sulfates, calcium, magnesium, carbonates, and so on to be removed. The conversion rate of this nanofiltration step is advantageously between 60 and 85%. It is noted in this regard that the conversion rate is equal to the ratio between the flow rate of permeate produced and the flow rate of concentrate at the inlet of the first demineralization unit  26 . 
     The implementation of such a nanofiltration step leads to the production of 60 to 85% of a permeate containing monovalent cations and anions, such as chlorides, sodium, potassium, etc., and 15 to 40% of a second concentrate containing divalent cations and anions, such as sulfates, calcium, magnesium, carbonates, and so on. 
     The permeate is discharged from the first demineralization unit  26  by means of the discharge pipe  27 . The second concentrate is extracted from this demineralization unit  26  via the extraction pipe  28 . 
     This second concentrate is then routed to the inlet of the second demineralization unit  29 . There, it undergoes demineralization by being placed in contact with ion exchange resins. 
     This demineralization on ion exchange resins enables the sulfates and other divalent cations and anions present in the second concentrate to be retained. 
     The permeate coming from the first demineralization unit  26  is recirculated inside the second demineralization unit  29  via the pipe  27 . This recirculation enables a regeneration of the ion exchange resins to be implemented. 
     Indeed, this permeate contains chlorides that were not eliminated during the passage of the first concentrate in the first demineralization unit. The ions attached to the resins during the treatment are exchanged against the chloride ions present in this permeate. The resin then returns to its initial state. 
     It is noted that the sodium chloride concentration is between 125 and 250 grams of NaCl per liter of resin. 
     The implementation of this second demineralization step leads to the production of a third concentrate and at least partially demineralized water. 
     This third concentrate is extracted from the second demineralization unit  29  and rejected into the natural environment via the extraction pipe  30 . 
     The at least partially demineralized water is discharged from the second demineralization unit  29  via the discharge pipe  31 . 
     The flow of an at least partially demineralized water is distributed between pipes  32  and  33 . 
     The portion of water circulating inside pipe  33  is directly mixed with the desalinated water circulating in pipe  22 . 
     The portion of water circulating in pipe  32  is routed to an inlet of the exchanger  24 . It circulates inside this exchanger so as to cool the first concentrate coming from the desalination unit  21 . The demineralized water is then discharged from the exchanger  24  and mixed via the pipe  34  with the desalinated water circulating in the pipe  22 . 
     The control and measurement means are implemented so as to measure the temperature of the first concentrate coming from the desalination unit  21  and compare the value of this temperature with a threshold value. These control means control the opening and closing of the solenoid valve  35  on the basis of this comparison. Thus, when the temperature of the first concentrate is above a certain threshold, the solenoid valve  35  is controlled so that a portion of the at least partially demineralized water flows into the pipe  32  and passes through the exchanger  24  so as to reduce the temperature of the first concentrate. Conversely, when the temperature of the first concentrate is below a certain threshold, the solenoid valve  35  is controlled so that all of the at least partially demineralized water flows into the pipe  33 . 
     The fact of cooling the first concentrate when its temperature becomes too high enables damage to the nanofiltration membranes housed in the first demineralization unit  26  to be prevented. 
     The means for measuring the salt concentration of the first concentrate and means for comparing the value measured with a threshold value are implemented so as to bypass (or shunt) the implementation of one or the other of the first and second demineralization units when the salt concentration of the first concentrate is low enough. 
     4. Tests 
     4.1 Demineralization 
     Tests have been conducted so as to determine the concentrations of species present in the permeates and concentrates generated by the implementation of a process according to the first embodiment of the invention. 
     The desalination installation implemented in the context of these tests was operated 24 hours per day and treated 1000 m 3 /day of water to be desalinated. 
     The installation comprised a plurality of reverse osmosis filtration units. It should be noted that the number of units was dependent on the amount of treated water to be produced. 
     In these tests, the flow rate of concentrate to be treated coming from the reverse osmosis was on the order of 550 m 3 /day. 
     The concentrates coming from the reverse osmosis were treated in a plurality of nanofiltration units. It should be noted that the number of units was dependent on the amount of concentrate to be treated. 
     The permeate coming from the nanofiltration was sent at a flow rate on the order of 330 m 3 /day to a storage tank to be used during the regeneration of ion exchange resins. 
     The volume of concentrate produced by the implementation of the nanofiltration was on the order of 220 m 3 /day. 
     During these tests, the ion exchange resin demineralization unit included a first and a second independent reactor mounted in series. The first reactor housed a mixture of strong cationic-type ion exchange resins and inert ion exchange resins. The second reactor housed a mixture of strong anionic-type ion exchange resins and inert ion exchange resins. It is also possible to envisage implementing ion exchange resins in a mixed bed. 
     The volume of the third concentrate coming from the regeneration of ion exchange resins was on the order of 30 m 3 /day. The volume of demineralized water collected from the ion exchange resin treatment was on the order of 300 m 3 /day. This water volume added to that coming from the reverse osmosis led to the production of around 750 m 3 /day of partially desalinated water. 
     The regeneration of ion exchange resins was implemented when the reverse osmosis units were stopped. The duration of these stops could range from 4 to 48 hours, which is sufficient for effective regeneration. 
     The regeneration of ion exchange resins was activated manually by actuation of a push-button. It could also be activated automatically once a predetermined volume of water to be treated is reached or when the conductivity at the outlet of the ion exchangers reaches a predetermined value. 
     The concentrations of species present in the permeates and concentrates generated during these tests are grouped in tables 2 and 3. 
     
       
         
               
             
               
               
               
               
               
             
               
               
               
               
               
             
           
               
                 TABLE 2 
               
             
             
               
                   
               
               
                 results of first demineralization 
               
             
          
           
               
                   
                   
                 First 
                 Second 
                   
               
               
                   
                 Parameters 
                 concentrate 
                 concentrate 
                 Permeate 
               
               
                   
                   
               
             
          
           
               
                   
                 Cations 
                   
                   
                   
               
               
                   
                 (mg/l) 
               
               
                   
                 Ca 2+   
                 840.1 
                 2,030 
                 28 
               
               
                   
                 Mg 2+   
                 2,616.3 
                 6,250 
                 101 
               
               
                   
                 Ba 2+   
                 1.90 
                 2.0 
                 0.9 
               
               
                   
                 Na 2+   
                 23,056.6 
                 49,580 
                 5,318 
               
               
                   
                 K +   
                 784.3 
                 455 
                 602 
               
               
                   
                 Sr +   
                 9.34 
                 10.6 
                 4 
               
               
                   
                 Anions 
               
               
                   
                 (mg/l) 
               
               
                   
                 Cl −   
                 41,046.02 
                 95,760 
                 4,568 
               
               
                   
                 SO 4   2−   
                 5,610.26 
                 13,890 
                 101 
               
               
                   
                 HCO 3   −   
                 311.29 
                 751 
                 18 
               
               
                   
                 NO 3   −   
                 1.87 
                 3.5 
                 0.65 
               
               
                   
                 Bore 
                 9.06 
                 15 
                 3 
               
               
                   
                   
               
             
          
         
       
     
     
       
         
               
             
               
               
               
               
               
             
               
               
               
               
               
             
           
               
                 TABLE 3 
               
             
             
               
                   
               
               
                 results of second demineralization 
               
             
          
           
               
                   
                   
                   
                   
                 Partially 
               
               
                   
                   
                 Second 
                 Third 
                 demineralized 
               
               
                   
                 Parameters 
                 concentrate 
                 concentrate 
                 water 
               
               
                   
                   
               
             
          
           
               
                   
                 Cations 
                   
                   
                   
               
               
                   
                 (mg/l) 
               
               
                   
                 Ca 2+   
                 2,030 
                 18,270 
                 203 
               
               
                   
                 Mg 2+   
                 6,250 
                 56,250 
                 625 
               
               
                   
                 Ba 2+   
                 2.0 
                 17 
                 0.3 
               
               
                   
                 Na 2+   
                 49,580 
                 490,000 
                 495 
               
               
                   
                 K +   
                 455 
                 4,000 
                 45 
               
               
                   
                 Sr +   
                 10.6 
                 100 
                 0.5 
               
               
                   
                 Anions 
               
               
                   
                 (mg/l) 
               
               
                   
                 Cl −   
                 95,760 
                 910,000 
                 4,790 
               
               
                   
                 SO 4   2−   
                 13,890 
                 125,000 
                 1,390 
               
               
                   
                 HCO 3   −   
                 751 
                 6,900 
                 75 
               
               
                   
                 NO 3   −   
                 3.5 
                 35 
                 — 
               
               
                   
                 Bore 
                 15 
                 149 
                 1 
               
               
                   
                   
               
             
          
         
       
     
     During these tests, the conversion rates of the first and second demineralization were respectively 60% and 90%. 
     It is clear from these tables that the partially demineralized water that is mixed with the desalinated water contains a certain proportion of salts initially present in the second concentrate. In this way, the third concentrate that is rejected into the natural medium contains fewer salts. 
     4.2 Production 
     A desalination technique, which, according to the prior art, implements a reverse osmosis treatment has a conversion rate of between 42 and 48%. In other words, this technique of the prior art enables between 42 and 48% desalinated water and between 52 and 58% concentrate to be produced. 
     A technique, which, according to the invention, implements reverse osmosis, then nanofiltration and finally a treatment on ion exchange resins has an overall conversion rate of between 55 and 75%. In other words, the technique of the invention enables between 55 and 75% desalinated water and between 25 and 45% concentrate to be produced. 
     Indeed, according to the invention, the efficiency of the nanofiltration is between 30 and 50%, while that of the treatment on ion exchange resins is between 50 and 70%. 
     Thus, at the end of the reverse osmosis, according to the invention, between 42 and 48% permeate are obtained. The concentrate, which represents between 52 and 58%, i.e. an average of 55%, is then treated by nanofiltration. Between 16.5 and 27.5% permeate and between 27.5 and 38.5% concentrate are then obtained. This concentrate is then treated on ion exchange resins. Between 13.75 and 26.95% at least partially demineralized water and between 11.55 and 13.75% concentrate are then obtained. 
     The technique according to the invention thus enables between 55, 75 and 74, 95% treated water (mixture of an at least partially desalinated water and an at least partially demineralized water) to be produced. 
     The technique according to the invention therefore enables an overall production of: 
     between 55 and 75% treated water, and 
     between 25 and 45% concentrate, 
     i.e. around 44% more treated water, and 
     36% less concentrate. 
     Advantages 
     The implementation of a process for treating water according to the invention has in particular the following advantages, by comparison with the prior art techniques. 
     First: 
     the amount of desalinated water produced is greater; 
     the volume of concentrate to be rejected into the natural environment is significantly reduced; 
     the external water consumption for the regeneration of ion exchange resins is zero. 
     The implementation of a treatment process according to the invention therefore enables the impact of water desalination on the environment to be reduced. 
     Second: 
     the permeate is used to regenerate the ion exchange resins; 
     damage to nanofiltration membranes is controlled by the implementation of the exchanger enabling the first concentrate to be cooled. 
     The implementation of a treatment process according to the invention also enables the costs of water desalination to be reduced.