System and method for water treatment

专利摘要:
A method of liquid treatment in a liquid treatment plant comprising at least one liquid treatment module employing at least one of reverse osmosis and nanofiltration membranes, wherein the at least one module has a liquid inlet, a permeate outlet and a brine outlet, wherein the method comprises: (a) supplying the liquid to be treated to the liquid treatment module through the liquid inlet; (b) providing at least a portion of the liquid from the brine outlet again towards the liquid inlet; (c) monitoring the liquid pressure within the at least one liquid treatment module; and (d) upon sensing that the liquid pressure exceeds a predetermined liquid pressure threshold, closing the liquid flow from the brine outlet back to the liquid inlet to reduce the liquid pressure in the at least one treatment module of liquid and performing simultaneously at least one of the following: (i) reducing the liquid pressure at the brine outlet to a level above atmospheric pressure that exceeds the osmotic pressure of the liquid in the at least one liquid treatment module ; (ii) increase the entry of liquid into the liquid inlet by using a designated volume of liquid at times other than when it is exceeded and immediately after; (iii) balancing the liquid pressures between a liquid pressure within the at least one liquid treatment module and within a liquid feed tank; and (iv) providing a return flow liquid passage which reduces the pressure from the liquid inlet of the at least one liquid treatment module which avoids a liquid pressure increase pump upstream of the liquid inlet. (Machine-translation by Google Translate, not legally binding)
公开号:ES2673945A2
申请号:ES201790032
申请日:2016-03-03
公开日:2018-06-26
发明作者:Benaya HOZ
申请人:Israel Aerospace Industries Ltd；
IPC主号:

专利说明:

SYSTEM AND METHOD FOR WATER TREATMENT
5 TECHNOLOGICAL FIELD
The present application refers to systems and methods for water treatment, in particular, the methods allow the continuous operation of a treatment plant.
10 BACKGROUND IN THE TECHNIQUE
Desalination processes and / or treatment processes are known in the art, and are configured to receive feedwater and, after proper treatment, produce a first stream of "produced" water (usually clean / fresh water) as well.
15 known as permeate, and a second stream of brine (usually very salty water).
Different systems and methods were devised to increase the performance of such treatment processes, including more sophisticated membranes, provisions of
20 water recirculation, etc.
Here are some examples:
US 7,628,921 describes an apparatus for desalination in closed circuit
25 consecutive sequential water and salt solution by reverse osmosis with at least one circuit and a single container (eN), in which the circuit includes at least one RO module (M 1) connected in parallel;
US 7,695,614 describes an apparatus for sequential continuous sequential desalination in closed circuit of a water and salt solution by reverse osmosis comprising a closed circuit system comprising one or more desalination modules with their respective inputs and outputs connected in parallel through conduit pipes, in which each of the desalination modules comprises one or more membrane elements, a pressurization device to create a counter pressure that allows desalination by reverse osmosis and the replacement of the permeate released by fresh water , a circulation system to recirculate the solution
desalinated through the desalination modules, a conduit pipe system to collect permeate from the desalination modules, a conduit pipe system to remove the brine effluent, a valve system to allow periodic discharge of the brine from the closed circuit without stopping the
5 desalination, and monitoring and control systems to allow the continuous desalination in closed circuit of the desired recovery to be carried out in consecutive sequential stages under conditions of constant or variable pressure;
US2008 / 217222 describes a modular unit apparatus for the continuous separation of suspended particles from fluids or supply solutions by a sequential process 10 in a closed circuit, comprising a closed circuit system comprising filter modules and transverse flow membrane with their respective inputs and outputs connected in parallel with each of the modules comprising a filter element and transverse flow membrane within a housing, a circulation system that allows the recirculation of the fluid or the supply solution through the 15 membrane, a conduit pipe system to supply said clean supply to the closed circuit, a conduit pipe system to collect permeate from the membrane modules, a conduit pipe system to remove fluids or solutions with suspended particles Closed circuit concentrates, two systems of valves to allow the connection or disconnection of said supply pipe of
20 fresh feed to the closed circuit, and to allow periodic discharge of the suspended solution from the closed circuit without stopping the filtration, and monitoring and control systems; Y
US 8,025,804 discloses an apparatus for sequential continuous sequential desalination in closed circuit of a water and salt solution by reverse osmosis comprising a closed circuit system comprising one or more desalination modules with their respective inputs and outputs connected in parallel through conduit pipes, in which each of the desalination modules comprises one or more membrane elements, a pressurization device to create a counter pressure that allows desalination by reverse osmosis and the replacement of the permeate released by fresh water , a circulation system to recirculate the desalinated solution through the desalination modules, a conduit pipe system to collect the permeate of the desalination modules, a conduit pipe system to remove the brine effluent, a system of valves to allow periodic discharge of the brine from the closed circuit without stopping the desalination, and monitoring and control systems to allow the desalination
Continuous closed circuit of the desired recovery is carried out in consecutive sequential stages under conditions of constant or variable pressure.
The recognition of the preceding references should not be construed as being5 are in some way relevant to the patentability of the subject described herein.
General description
The present invention seeks to provide water treatment methods and systems.
10 improved. Therefore, according to an embodiment of the present invention, a liquid treatment method is provided which includes supplying the liquid to be treated at least to a liquid treatment module that employs at least one of reverse osmosis membranes and membranes. nanofiltration, in which the at least one module has a liquid inlet, a permeate outlet and a brine outlet, monitor the pressure
15 of the liquid within the at least one liquid treatment module and after it exceeds a liquid pressure threshold in the at least one liquid treatment module, which represents the excess of a salinity threshold in the liquid therein, reduce the pressure of the liquid in the at least one liquid treatment module by performing at least one of the following functions: open a liquid pressure reduction valve at the outlet
Brine 20, thereby reducing the pressure of the liquid in the brine outlet to a level higher than the atmospheric pressure that exceeds the osmotic pressure of the liquid in the at least one liquid treatment module, increasing a liquid volume output of a circulation pump that removes the brine from at least one liquid treatment module and supplies the liquid to the water inlet from a volume outlet of
25 at a time other than when it is exceeded and immediately after this, balance the liquid pressures between a liquid pressure within the at least one liquid treatment module and within a liquid feed tank, and open a valve reduction of liquid pressure in the liquid inlet, thereby providing a return flow liquid passage that reduces the pressure from the inlet of
At least one liquid treatment module that avoids a liquid pressure booster pump upstream of the liquid inlet.
According to an embodiment of the present invention, after a liquid pressure threshold in the at least one liquid treatment module is exceeded, which
35 represents the excess of a salinity threshold in the liquid in this, the pressure is reduced
of the liquid in the at least one liquid treatment module when performing at least two of the following functions: opening a liquid pressure reducing valve at the brine outlet, thereby reducing the pressure of the liquid at the outlet of brine to a level higher than the atmospheric pressure that exceeds the osmotic pressure of the liquid in the at least one liquid treatment module, increase a liquid volume output from a circulation pump that removes the brine from the at least one module of liquid treatment and supplies the liquid to the water inlet from a liquid volume outlet at times other than when it is exceeded and immediately after this, balance the liquid pressures between a liquid pressure within the at least one
10 treatment module and within a liquid feed tank, and open a liquid pressure reducing valve at the liquid inlet, thereby providing a liquid flow passage return that reduces the pressure from the inlet of liquid from at least one liquid treatment module that avoids a liquid pressure booster pump upstream of the liquid inlet.
According to an embodiment of the present invention, after a liquid pressure threshold in the at least one liquid treatment module is exceeded, which represents the excess of a salinity threshold in the liquid in it, it is reduced the liquid pressure in the at least one liquid treatment module when carrying out at least three
20 of the following functions: open a liquid pressure reduction valve at the brine outlet, thereby reducing the pressure of the liquid at the brine outlet to a level higher than the atmospheric pressure that exceeds the osmotic pressure of the liquid in the at least one liquid treatment module, increase a liquid volume output of a circulation pump that removes the brine from the at least one treatment module of
25 liquid and supplies the liquid to the water inlet from a liquid volume outlet at times other than when it is exceeded and immediately after this, balance the liquid pressures between a liquid pressure within the at least one module of liquid treatment and inside a liquid feed tank, and open a liquid pressure reducing valve at the liquid inlet, providing
Thus, a return flow liquid passage that reduces the pressure from the liquid inlet of the at least one liquid treatment module that avoids a liquid pressure booster pump upstream of the liquid inlet.
According to an embodiment of the present invention, after a liquid pressure threshold is exceeded in the at least one liquid treatment module, which
represents the excess of a salinity threshold in the liquid in it, the liquid pressure in the at least one liquid treatment module is reduced by performing all of the following functions: opening a liquid pressure reduction valve in the brine outlet, thereby reducing the pressure of the liquid in the brine outlet to a level 5 higher than the atmospheric pressure that exceeds the osmotic pressure of the liquid in the at least one liquid treatment module, increasing a volume output of liquid from a circulation pump that removes the brine from at least one liquid treatment module and supplies the liquid to the water inlet from a liquid volume outlet at times other than when it is exceeded and immediately after this, 10 balance the liquid pressures between a liquid pressure within the at least one liquid treatment module and within a feed tank d e liquid, and opening a liquid pressure reduction valve at the liquid inlet, thereby providing a return flow liquid passage that reduces the pressure from the liquid inlet of the at least one liquid treatment module that avoid a booster pump
15 of liquid pressure upstream of the liquid inlet.
According to another embodiment of the present invention, a liquid treatment method is also provided which includes: supplying at least one water treatment module that includes at least one membrane and has a feed water inlet on one side of feeding of the at least one membrane, a permeate outlet on a permeate side of the at least one membrane and a brine outlet on a brine side of the at least one membrane, pressurizing the feed water supplied to the inlet of feedwater by using a pump that normally maintains a fixed outlet feedwater volume, regardless of the variations in the water pressure at an outlet thereof, in which the pump's energy consumption depends on variations in the water pressure at the outlet, monitor the water pressure at the pump outlet and, when a predetermined high pressure threshold is reached in the pump outlet, make changes immediately in the water supply to the module, to thereby cause the
30 Immediate decrease in water pressure at the pump outlet, to a pressure lower than the osmotic pressure on the supply side of a part but not the entire module, thereby immediately reducing the energy consumption of the pump , thereby providing savings in total energy costs per unit of treated water.
In accordance with yet another embodiment of the present invention, there is provided a method for the treatment of liquid in at least one liquid treatment module that includes at least one high pressure pump and a circulation pump, in which the method includes , after an operating threshold representing the excess of a salinity threshold in the at least one liquid treatment module is reached, perform the following: remove the brine from the at least one liquid treatment module and reduce, to an improved speed, the pressure of the liquid in the at least one liquid treatment module by at least one of the following: open a pressure reducing valve downstream of the high pressure pump, increase the volume output of the pump 10 circulation from its volume output when it functions as a concentrate circulation pump to a larger volume output when it functions as an ag pump ua feed, and pass the liquid from downstream of the high pressure feed pump upstream of the high pressure feed pump, the passage of liquid from downstream of the high pressure feed pump to stream
15 above the high pressure feed pump includes passing the liquid through a flow restrictor arranged in parallel with respect to the high pressure feed pump.
According to an embodiment of the present invention, the pressure of the liquid in the at
At least one liquid treatment module is reduced at an improved speed by at least two of the following: open a pressure reducing valve downstream of the high pressure pump, increase the volume output of the circulation pump from from its volume output when it functions as a concentrate circulation pump to a larger volume output when it functions as a water pump
25 feed, and pass the liquid from downstream of the high pressure feed pump upstream of the high pressure feed pump. Alternatively, the liquid pressure in the at least one liquid treatment module is reduced at an improved rate by all of the following: opening a pressure reducing valve downstream of the high pressure pump, increasing the output of
30 volume of the circulation pump from its volume output when it functions as a concentrate circulation pump to a greater volume output when it functions as a feed water pump, and the liquid is passed from downstream of the pump high pressure feed upstream of the high pressure feed pump, the liquid treatment module is a module of
Water treatment that includes at least one of at least one reverse osmosis membrane and at least one nanofiltration membrane and is operative for the treatment of at least one of seawater, brackish water and wastewater.
According to another embodiment of the present invention, there is even further provided a
5 water treatment system that includes: at least one operating liquid treatment module to receive feed water at a water inlet of this and to separate the feed water into permeate and concentrate, in which the permeate constitutes the water treated, the at least one liquid treatment module has a brine outlet to release the concentrate whose salinity is such that an operating threshold of the
10 system, a liquid pressure reduction valve at the brine outlet, a high pressure pump, which functions to pressurize the liquid to be treated received at a liquid feed inlet and to provide pressurized feed water outlet to the minus a liquid treatment module, a feed water flow sensor located upstream of the high pressure pump and that provides a
15 feed water flow output, a pump controller that receives the feed water flow output and controls the operation of the high pressure pump, a liquid pressure sensor to provide an indication of the output pressure of liquid in at least one of an inlet to at least one liquid treatment module, an outlet of the at least one liquid treatment module and within the at least one
20 liquid treatment module, a circulation pump that removes the brine from at least one liquid treatment module and supplies liquid to the water inlet, a liquid feed tank, a system controller that receives at least the indication of liquid pressure output within the at least one liquid treatment module, in which the system controller is operative, after exceeding a
25 liquid pressure threshold in the at least one liquid treatment module, which represents the excess of a salinity threshold in the liquid in it, reduce the liquid pressure in the at least one liquid treatment module when performing at least one of the following functions: open a liquid pressure reduction valve at the brine outlet, thereby reducing the liquid pressure at the brine outlet to a
30 level higher than the atmospheric pressure that exceeds the osmotic pressure of the liquid in the at least one liquid treatment module, increase a liquid volume output from a circulation pump that removes the brine from the at least one liquid treatment module and supplies the liquid to the water inlet from a liquid volume outlet at times other than when it is exceeded and immediately after this,
35 balancing the liquid pressures between a liquid pressure within the at least one treatment module and within a liquid feed tank, and opening a liquid pressure reducing valve at the liquid inlet, thereby providing a return flow liquid passage that reduces the pressure from the liquid inlet of the at least one liquid treatment module that avoids a pressure booster pump of
5 liquid upstream of the liquid inlet.
According to an embodiment of the present invention, the system controller is operative, after a liquid pressure threshold in the at least one liquid treatment module is exceeded, which represents the excess of a salinity threshold in the 10 liquid in this, to reduce the pressure of the liquid in the at least one liquid treatment module when performing at least two of the following functions: open the liquid pressure reduction valve at the brine outlet, reducing from that way the pressure of the liquid in the brine outlet to a level higher than the atmospheric pressure that exceeds the osmotic pressure of the liquid in the at least one liquid treatment module, 15 increasing a liquid volume output of the circulation pump which removes the brine from at least one liquid treatment module and supplies the liquid to the water inlet from a liquid volume outlet at times of di When it is exceeded and immediately after this, balance the liquid pressures between a liquid pressure within the at least one liquid treatment module and inside the tank of
20 feeding liquid, and opening a liquid pressure reducing valve at the liquid inlet, thereby providing a liquid flow passage return that reduces the pressure from the liquid inlet of the at least one treatment module of liquid that prevents a high pressure pump upstream of the liquid inlet.
25 Alternatively, the system controller is operative, after a liquid pressure threshold in the at least one liquid treatment module is exceeded, which represents the excess of a salinity threshold in the liquid therein, to Reduce the liquid pressure in the at least one liquid treatment module by performing at least three of the following functions: open the liquid pressure reduction valve at the outlet
30 brine, thereby reducing the pressure of the liquid in the brine outlet to a level higher than the atmospheric pressure that exceeds the osmotic pressure of the liquid in the at least one liquid treatment module, increasing a liquid volume output of the circulation pump that removes the brine from the at least one liquid treatment module and supplies the liquid to the water inlet from a volume outlet of
At a time other than when it is exceeded and immediately after this, balance the liquid pressures between a liquid pressure within the at least one liquid treatment module and inside the liquid feed tank, and open a reduction valve of liquid pressure at the liquid inlet, thereby providing a return flow liquid passage that reduces the pressure from the inlet of
5 liquid from at least one liquid treatment module that avoids a high pressure pump upstream of the liquid inlet.
In another alternative embodiment, the system controller is operative, after a liquid pressure threshold in the at least one liquid treatment module is exceeded, 10 which represents the excess of a salinity threshold in the liquid in it, To reduce the liquid pressure in the at least one liquid treatment module, perform all of the following functions: open the liquid pressure reduction valve at the brine outlet, thereby reducing the liquid pressure at the outlet of brine to a level higher than the atmospheric pressure that exceeds the osmotic pressure of the liquid in the at least one liquid treatment module, increase a liquid volume output from the circulation pump that removes the brine from the at least one module of liquid treatment and supplies the liquid to the water inlet from a liquid volume outlet at different times than when it is exceeded and immediately After this, balance the liquid pressures between a liquid pressure within at least one
20 liquid treatment module and inside the liquid feed tank, and open a liquid pressure reduction valve at the liquid inlet, thereby providing a return flow liquid passage that reduces the pressure from the inlet of liquid from at least one liquid treatment module that avoids a high pressure pump upstream of the liquid inlet.
In accordance with even another embodiment of the present invention, a water treatment system is still provided that includes at least one water treatment module that includes at least one membrane and has a feed water inlet on one side of feeding the at least one membrane, a permeate outlet on one side of
30 permeate of the at least one membrane and one brine outlet on one brine side of the at least one membrane, a high pressure pump, which normally maintains a fixed outlet feed water volume regardless of variations in pressure of the water at an outlet thereof, a system controller that receives at least the indication of liquid pressure output within the at least one treatment module
35 of liquid, in which the system controller is operational, after exceeding a
liquid pressure threshold in the at least one liquid treatment module, which represents the excess of a salinity threshold in the liquid in it, to reduce the liquid pressure in the at least one liquid treatment module when performing at least one of the following functions: pressurize the feed water supplied to the inlet of 5 feed water by using the high pressure pump, in which the energy consumption of the pump depends on the variations in the pressure of the water at the outlet, monitor the water pressure at the pump outlet and, when a predetermined high pressure threshold is reached at the pump outlet, immediately make changes in the water supply to at least one water treatment module liquid, to cause that
I am killed by the immediate decrease of the water pressure at the outlet of the high pressure pump, to a pressure lower than the osmotic pressure on the feed side of a part but not all of the at least one liquid treatment module, thereby immediately reducing the energy consumption of the high pressure pump, thereby providing savings in total energy costs per unit of treated water.
In accordance with even another embodiment of the present invention, a water treatment system is still provided that includes at least one water treatment module that includes at least one membrane and has a feed water inlet on one side of feeding the at least one membrane, a permeate outlet on one side of
Permeate of the at least one membrane and one brine outlet on one brine side of the at least one membrane, a high pressure pump, which normally maintains a fixed outlet feed water volume regardless of variations in pressure of the water at an outlet of this, a pressure reducing valve downstream of the high pressure feed pump, a circulation pump, a flow controller
A system that receives at least the indication of liquid pressure output within the at least one liquid treatment module, in which the system controller is operative, after a threshold of the liquid pressure in the system is exceeded. at least one liquid treatment module, which represents the excess of a salinity threshold in the liquid in it, to reduce the pressure of the liquid in the at least one treatment module
30 of liquid when performing at least one of the following functions: after an operating threshold that represents the excess of a salinity threshold in the at least one liquid treatment module occurs, perform the following: remove the brine from the less a liquid treatment module and reduce, at an improved rate, the pressure of the liquid in the at least one liquid treatment module by at least one of the
35: open the pressure reducing valve downstream of the high pressure feed pump, increase the volume output of the circulation pump from its volume output when it functions as a concentrate circulation pump to an outlet larger volume when it functions as a feed water pump, and the liquid passes from downstream of the high pressure feed pump upstream of the high pressure feed pump, the water treatment system also includes a restrictor of flow arranged in parallel with respect to the high pressure feed pump and the passage of the liquid from downstream of the high pressure feed pump upstream of the high pressure feed pump includes passing the liquid through the restrictor flow.
In accordance with an embodiment of the present invention. The liquid pressure in the at least one liquid treatment module is reduced at an improved rate by at least two of the following: open the pressure reducing valve downstream of the high pressure feed pump, increase the output of volume of the circulation pump from its volume output when it functions as a concentrate circulation pump to a larger volume output when it functions as a feed water pump, and the liquid passes from downstream of the feed pump high pressure upstream of the high pressure feed pump. Alternatively, the liquid pressure in the at least one liquid treatment module is reduced at an improved rate by at least three of the following: open the pressure reducing valve downstream of the high pressure feed pump, increase the volume output of the circulation pump from its volume output when it functions as a concentrate circulation pump to a larger volume output when it functions as a feed water pump, and pass the liquid from downstream of the high pressure feed pump upstream of the high pressure feed pump.
BRIEF DESCRIPTION OF THE DRAWINGS
In order to better understand the subject matter described herein and to exemplify how it can be carried out in practice, embodiments are described below only by way of non-limiting example, with reference to the attached drawings, in which:
Figure 1 is a simplified illustration of a water treatment system constructed and operative in accordance with an embodiment of the present invention;
Figures 2A and 2B are simplified illustrations of examples of periodic variations in feedwater pressure and osmotic pressure in embodiments of the system of Figure 1, in which each shows a difference from the prior art;
Figures 3A, 3B, 3e and 3D are simplified illustrations of liquid flows in the system of Figure 1 at various stages in the periodic variation in feedwater pressure and osmotic pressure shown in Figure 2A according with an embodiment of the present invention;
Figures 4A, 4B, 4C and 4D are simplified illustrations of liquid flows in the system of Figure 1 at various stages in the periodic variation in feedwater pressure and osmotic pressure shown in Figure 2A according with another embodiment of the present invention;
Figures 5A, 5B Y are simplified illustrations of liquid flows in the system of Figure 1 at various stages in the periodic variation in feedwater pressure and osmotic pressure shown in Figure 2A according to even another embodiment of the present invention;
Figures SA, 6B, 6e and 6D are simplified illustrations of liquid flows in the system of Figure 1 at various stages in the periodic variation in feedwater pressure and osmotic pressure shown in Figure 28 according with yet another embodiment of the present invention;
Figures 7A, 7B, 7e and 7D are simplified illustrations of liquid flows in the system of Figure 1 at various stages in the periodic variation in feedwater pressure and osmotic pressure shown in Figure 28 according with a further embodiment of the present invention;
Figures 8A, 8B, 8e and 8D are simplified illustrations of liquid flows in the system of Figure 1 at various stages in the periodic variation in the water pressure of
feed and osmotic pressure shown in Figure 28 according to even a further embodiment of the present invention;
Figures 9A, 9B, 9C and 90 are simplified illustrations of liquid flows in the
5 system of Figure 1 at various stages in the periodic variation in the water pressure offeed and osmotic pressure shown in Figure 2A according to even afurther embodiment of the present invention;
Figures 10A, 10B, 10C and 100 are simplified illustrations of liquid flows in the
10 system of Figure 1 at various stages in the periodic variation in feedwater pressure and osmotic pressure shown in Figure 2A according to an alternative embodiment of the present invention; Y
Figures 11A, 11B, 11C and 110 are simplified illustrations of liquid flows in the
The system of Figure 1 in various stages in the periodic variation in feedwater pressure and osmotic pressure shown in Figure 28 in accordance with a further embodiment of the present invention.
DETAILED DESCRIPTION OF EMBODIMENTS
Reference is now made to Figure 1, which is a simplified illustration of a liquid treatment system constructed and operative in accordance with an embodiment of the present invention, and to Figures 2A and 28, which are illustrations of timelines. simplified examples of the operation of the system of Figure 1, in which
25 desalinate seawater.
The liquid treatment system of Figure 1 comprises at least one liquid treatment module, the water treatment module 100 comprises reverse osmosis membranes and / or nanofiltration membranes. The system in Figure 1 is operational
30 for the treatment of the liquid to be treated, such as feedwater, which may be, for example, seawater, brackish water or wastewater.
The water treatment module 100 is described in the US patent application
No 13 / 603.028 of the applicant, filed on September 4, 2012 with the title: SYSTEM AND METHOD FOR DESALLNATION OF WATER, and published as U.S. Patent Application Published No. 2014/0061129 on 6 March 2014, the description of which is incorporated herein by reference.Figure 2A in US Patent Application No. 13 / 603,028 illustrates a water treatment module, which is hereby designated by the
5 reference number 100.
For the purposes of the description that follows, the following definitions will be used: feedwater - water to be treated by the system, such as saline, seawater, brackish water or wastewater;
10 mixed feed water - water supplied to the water treatment module 100, which may include feed water and water that was previously treated in the water treatment module 100 and is re-supplied to the water treatment module for further treatment; water from module feed side - water on a feed side, which is
15 differs from a permeate side of module 100. The salinity of the module feed side water increases as the module feed side water passes through the module, from an initial salinity, which represents the mixed feed water salinity, up to a concentrated salinity, which represents the salinity of the concentrate outlet at an outlet on the feed side, which differs from the side
20 permeate, from module 100.
An inherent feature of the water treatment modules 100 is that the osmotic pressure on the feed side of these increases over time as the salinity on the feed side increases up to a certain point in time.
25 which reduces the salinity on the feeding side, which reduces the osmotic pressure. As described hereinafter, the salinity of the mixed feed water on the feed side is reduced by supplying feed water alone instead of a mixture of feed water and recirculated concentrate.
30 An increase in osmotic pressure requires a corresponding increase in water pressure on the feed side of module 100 to maintain permeate production. This increase is automatically provided by a high pressure pump 102, operative to pressurize the liquid to be treated up to typical pressures of about 15 bar for brackish water and up to about 70 bar for sea water.
The high pressure pump 102 may be any suitable type of pump, such as a positive displacement pump. An example of a positive displacement pump is a Danfoss APP 21-43 high pressure pump, commercially available from Danfoss NS Nordborgvej 81, 6430 Nordborg, Denmark. The high pressure pump 102 is
5 controlled by the output of a feed water flow sensor 104 upstream of the pump 102, which is received by a pump controller 106, for example, an ABB ACS800-U1 controller, commercially available from ABB Inc. MS 3L7 29801 Euclid Ave, Wickliffe, OH 44092-2530, USA.
10 A mixed feed water pressure sensor 108 is provided on the feed side of the module 100. A typical graph of the mixed feed water pressure, as measured by the pressure sensor 108 as a function of time and with respect at the osmotic pressure on the supply side of the module 100, it appears in an enlarged part of Figure 1 and in Figures 2A and 2B. Alternatively or additionally, you can
A water pressure sensor is provided at a suitable location within module 100 or at an outlet of the module to measure the pressure of the liquid flowing through it. The variation of the feedwater pressure as a function of time usually has a periodicity of a few minutes, usually between 3 -30 minutes in the desalination of seawater and possibly greater in the desalination of brackish water.
20 As seen in Figure 1, the water treatment module includes multiple pressure vessels 110 arranged in parallel. Each pressure vessel 110 includes, for example, multiple membrane elements 112, usually an amount of eight, of which only four are shown in the drawing for the purpose of brevity. Pressure vessels 110 are commercially available from various suppliers, for example,
25 BEL Composite Industries Ud, Industrial Zone, Kiryat Yehudit, P.O.B. 4, 84100 Beer Sheva, Israel, and membrane elements 112 are commercially available from various suppliers, for example, LG NanoH20, 750 Lairport Street, El Segundo, CA 90245. The liquid to be treated is supplied at a feed inlet of liquid and is pressurized by a high pressure pump 102, operative to pressurize the liquid to be treated until
30 typical pressures of approximately 15 bar for brackish water and up to approximately 70 bar for seawater. The liquid to be treated, referred to hereinafter as feedwater, where the definition of "feedwater) comprises, among other things, saline solution, brackish water, seawater and wastewater, is supplied by a
35 feed manifold 114 to parallel pressure vessels 110. The treated water, referred to hereinafter as "permeate", where the definition of "permeate" comprises, among other things, "produced water) ), of each of the pressure vessels 110, is supplied by a permeate manifold 116 to a permeate outlet 118.
The concentrate of each of the pressure vessels 110 is supplied by a concentrate manifold 120 to a recirculation duct 122, which directs the concentrate back to the feed manifold 114, downstream of the pump 102, by a control valve of recirculation 124 by using a circulation pump 126. A concentrate pressure sensor 128, a concentrate conductivity sensor 129 and a concentrate flow sensor 130 are provided downstream of the concentrate manifold 120.
The concentrate from the module 100 can also be provided from the pressure vessels 110 by the concentrate manifold 120 to a brine outlet 132 via a brine outlet control valve 134 for washing. Here, the concentrate that exits the module 100 and does not recirculate is called brine, the salinity of the brine that is washed is greater than the salinity of the concentrate that is recirculated through the conduit 122.
In some embodiments of the present invention, the brine of each of the pressure vessels 110 may be supplied from the concentrate manifold 120 through an auxiliary brine replacement conduit 136, an auxiliary tank feed conduit 138 and a control valve From replacement of auxiliary brine 140 to an auxiliary feed water tank 142, the salinity of the brine supplied to the auxiliary feed water tank 142 exceeds the salinity of the concentrate that is recirculated through the conduit 122.
It is noted that, as described herein below, the decision to recirculate the liquid as a concentrate or to wash the liquid as a brine may occur depending on the salinity of the liquid, as a function of the pressure of the liquid, as a function of a rate of the accumulation of contaminants in the membrane elements, a nominal value of system energy efficiency or it can be based on a predetermined schedule or any other suitable method. Additionally or alternatively, the selection of the threshold
it can be predetermined at a suitable threshold that will prevent or minimize the precipitation of contaminants in membrane elements 112 in module 100.
During the brine wash, the recirculation control valve 124 is closed. He
5 auxiliary feed water tank 142 is filled, before the opening of the auxiliary brine replacement control valve 140, with feedwater by means of an auxiliary feedwater pump 144. The brine driven by the circulation pump 126 conducts the feed water from the auxiliary feed water tank 142 to the feed manifold 114 through a water line of
10 auxiliary feed 146 and an auxiliary feed water control valve 148. An auxiliary water flow sensor 150 is provided upstream of the auxiliary feed water tank 142. After the complete replacement of the brine with feed water in the module 100, the recirculation control valve 124 is opened and the auxiliary brine replacement control valve 140 and the water control valve of the
15 auxiliary feed 148. Next, the auxiliary feed water pump 144 fills the auxiliary feed water tank 142 with feed water, which leads the brine to an auxiliary brine outlet 152 via an outlet tank control valve of auxiliary brine 154.
20 It is noted that, alternatively, elements 136-154 can be ignored.
In some embodiments of the present invention, the water pressure on the feed side of the module 100 can be rapidly reduced at desired times by operating a recycle duct control valve 156 to redirect the water.
Feed 25 from downstream of the high pressure feed pump 102 upstream of the pump 102 through a conduit 158 and through a flow restrictor 160, which limits the pressure reduction to a pressure greater than the pressure atmospheric, in which said pressure exceeds the osmotic pressure of the feed water on the feed side of the module 100.
In accordance with an embodiment of the present invention, a feed pressure management (FPM) controller 162 is provided, which controls the operation of the high pressure feed pump 102, the circulation pump 126 , auxiliary feed water pump 144, recirculation control valve 35 124, brine outlet recirculation control valve 134, control valve
replacement auxiliary brine 140, auxiliary feed water control valve 148, auxiliary brine outlet tank control valve 154, and recycle duct control valve 156 to adjust the pressure at which the desalination in the at least one water treatment module.
5 As can be seen in Figures 2A and 2B, which will be described in detail below, and which refer to examples in which seawater is desalinated, periodic variations in feedwater pressure during water treatment correspond to periodic variations in osmotic pressure, which corresponds to the
10 salinity of the feed water supplied to the module 100, as can be measured by a conductivity sensor (not shown) usually downstream of the pressure sensor 108.
The control of the variation of the feedwater pressure can be achieved by several
15 ways, such as according to the flow rate measured by the flow sensor 104 and, alternatively or additionally, according to the salinity of the water supplied to the feed side of the module 100, which may include the feed water received from the pump 102, the recirculated water received from the recirculation conduit 122, the auxiliary feed water received by the auxiliary conduit 146 and combinations thereof.
20 Alternatively, the supply pressure can be varied according to a predetermined schedule. As a further alternative, the desired feed pressure can be achieved by using the recycling duct 158 with or without the flow restrictor 160. Other alternative methodologies can be employed for controlling the variation of the feed pressure.
25 The FPM controller 162 is operative to periodically open and close the recirculation control valve 124, the brine outlet control valve 134, the auxiliary brine replacement control valve 140, the feedwater control valve auxiliary 148, auxiliary brine outlet tank control valve 154 and valve
30 of recycle duct control 156 according to a predetermined schedule or, alternatively, for example, in response to the detected salinity of the concentrate, for example, by means of an outlet of the sensor 129, or the excess of a threshold of predetermined maximum feed pressure, for example, by an output of sensor 108 or sensor 128.
The FPM controller 162 is also operative to periodically activate the auxiliary feed water pump 144 and can also be operative to change the flow of the circulation pump 126. Other alternative algorithms can be used to control the opening and closing of the valve recirculation control 124, the control valve
5 brine outlet 134, auxiliary brine replacement control valve 140, auxiliary feed water control valve 148, auxiliary brine outlet tank control valve 154 and recycle duct control valve 156 , and to control the operation of the high pressure feed pump 102, the circulation pump 126 and the auxiliary feed water pump 144.
In some embodiments of the invention, once the concentration of concentrate is increased to a predetermined level for which it is considered that continuous water treatment is not practicable, the FPM controller 162 opens the auxiliary brine replacement control valve. 140 and allows the brine to flow from the collector of
15 concentrate 120, by the auxiliary brine replacement conduit 136 and the auxiliary tank feed water conduit 138, towards the auxiliary feed water tank 142. In some embodiments of the invention, the FPM controller 162 also closes the recirculation control valve 124 at approximately the same time. The volume of brine flowing out of the system can be measured by the sensor
20 of concentrate flow 130. The feed water that is in the auxiliary feed water tank 142 is conducted by the circulation pump 126 so that it already flows through the auxiliary feed water line 146 and the control valve of auxiliary feed water 148 to the feed manifold 114. The feedwater, with a salinity significantly lower than that of the brine, enters the
25 module 100.
Various methodologies are described below to ensure that the feedwater pressure is higher than the atmospheric pressure and higher than the osmotic pressure of the feedwater on the feed side of the module 100 at all times, with reference to Figures 2A and 28 And Figures 3A -11 D. Ensuring that the feedwater pressure remains higher than the atmospheric pressure and exceeds the osmotic pressure of the feedwater on the feed side of the module 100 prevents overshoot of the feed pressure when the feed water of the high pressure feed pump 102 enters module 100, said overshoot produces
35 commonly in prior art systems.
It is noted that the term "overshoot", as used herein, refers to operating the high pressure feed pump 1 02 at an excessively high pressure relative to the osmotic pressure of the feed water, which usually This occurs when the controller causes the system to supply feed water, such as from auxiliary feed water tank 142, instead of recirculated concentrate to modules 1 00, without changing the pressure of the feed water supplied by the pump high pressure feed 102. The operation of the high pressure feed pump 102 at an excessively high pressure relative to
1 O at the osmotic pressure of the feed water increases the energy needed to operate the system.
In the following description, it will be noted that the pressure values provided for the various embodiments described below and are shown in Figures 2A and
15 28 are values associated with desalination of seawater by membrane. Different pressure values will be applied to the desalination of brackish water and other types of feedwater.
During normal operation in steady state of the system, before the start of a
20 periodic process to replace the concentrate in the water treatment module 100 with feed water, the brine outlet control valve 134, the auxiliary brine replacement control valve 140, the auxiliary feed water control valve 148, the auxiliary brine outlet tank control valve 154 and the recycle duct control valve 156 are all closed and the control valve of
25 recirculation 124 is open.
During normal operation in steady state, the concentrate of the concentrate manifold 120 is again directed towards the inlet of the feed manifold 114 through the recirculation conduit 122 and the recirculation control valve 124, such as shown in Figure 1 by means of an arrow with the CONCENTRATE label, which represents the recirculation flow in the recirculation duct 122. In the feed manifold 114, the concentrate is mixed with feedwater, as shown in Figure 1 by means of an arrow with the MIXED label, which represents the mixed flow in the feed manifold 114, and the mixed flow enters the pressure vessels 110 of the module 100 for treatment. The flow described above during operation
normal steady state is represented by continuous black lines in the
Figures 3A, 4A, SA, 6A, 7A, BA, 9A, 10A AND 11A.
Feed pressure gradually increases as the salinity of the
5 mixed water supplied to the membrane elements 112. Once the concentrationof concentrate increases to a predetermined level for which theContinuous water treatment is not practicable, the periodic process begins toreplace the concentrate in the water treatment module 100 with water fromfeeding. Figures 3A-11 D illustrate various techniques to replace the concentrate
10 in the water treatment module 100 with feed water at a pressure higher than the atmospheric pressure, which exceeds the osmotic pressure of the feed water on the feed side of the module 100 without causing overshoot.
Usually, the predetermined level of concentrate concentration that is considered
15 not practicable to continue treatment depends on one of several operational considerations, such as the rate of accumulation of pollutants and energy efficiency. Reference is now made to Figure 2A, which illustrates the periodic variations in the pressure of mixed feed water, as measured by pressure sensor 108, and in the osmotic pressure of mixed feed water, the existence of which is estimated at
20 pressure sensor 108 when the circulation pump 126 operates at a normal pumping rate. The osmotic pressure of mixed feed water estimated at the pressure sensor 108 generally depends on the salinity of the water on the feed side of the membranes 112 in the module 100.
25 Periodic variations in the pressure of mixed feed water during water treatment correspond to periodic variations in the salinity of the feed water entering module 100, as can be measured by the conductivity sensor, usually located downstream of the pressure sensor 108. The y axis represents the pressure in seawater desalination and the x axis represents time.
30 The dashed vertical lines "A" represent points in time at which a threshold is reached, such as a maximum feed water pressure threshold.
When the threshold is reached, the pressure vessels 110 are still full of concentrate, whose salt concentration continues to increase as it moves to
35 through the pressure vessel. Therefore, the osmotic pressure of the mixed feed water and the pressure of the mixed feed water continue to increase until the feed water enters the pressure vessels 110 to replace the concentrate in these. Usually, when the threshold is reached, the system begins the brine washing process.
In Figures 2A and 28, the osmotic pressure line of mixed feed water 170 represents the estimated osmotic pressure of the mixed feed water. Therefore, when the feed water of the pump 102 is mixed with the concentrate of the recirculation duct 122, the mixed osmotic pressure gradually increases, as observed in the gradual slope of the line 170. Once it is reached A threshold, such as a salinity threshold or a pressure threshold, controller 162 begins the washing process. During the washing process, the concentrate is not recirculated back to the feed manifold 114, therefore, only the feedwater enters the feed manifold 114 and the mixed osmotic pressure decreases rapidly, such
15 as shown in the steep decrease in line 170.
Line 175 in Figure 2A illustrates the behavior of the mixed feed water pressure in the prior art, represented by the teachings of U.S. Patent No. 8,025,804. As can be seen, the feedwater pressure line
20 mixed 175 begins its fall (represented by the dotted line to the right of the dotted line A) only after the osmotic pressure has already fallen below a certain threshold.
In contrast, line 180 illustrates the mixed feed water pressure of the present
25, which is controlled by the controller so that the mixed feed water pressure necessary for the desalination process by reverse osmosis is maintained not only during the gradual increase of the mixed feed water pressure, when the concentrate is recirculated back to the feed manifold 114, but also when the brine is washed in the pressure vessels 110 by means of the
30 feed water feed alone without recirculated concentrate.
One of the advantages of the present arrangement is the conservation of energy because the feed pump is not required to continue increasing the pressure (it can reduce the pressure before) - the pump in the disposition of the present application begins its fall in the dotted line A, considerably earlier with respect to the osmotic pressure,
compared to line 175 of the prior art. The difference, represented by the bounded area between line 175 and line 180, illustrates the energy benefit of operating at lower pressures for seawater desalination, therefore, saves energy. In both Figures 2A and 28, line 190 illustrates the osmotic pressure of the water on the side of
5 module power.
As further described below, Figure 28 is similar to Figure 2A, with the exception that the values are provided for the embodiment in which the circulation pump 126 operates at a pumping rate greater than normal, that generates a
10 major flow.
Reference is now made to Figures 3A -3D, which are simplified illustrations of water flows in a first embodiment of the water treatment system of the type shown in Figure 1.
15 Figure 3A shows the flow, during normal steady state operation of the system, in continuous black color.
Figure 38 shows, in continuous black lines, the flow that occurs once the
Concentrate concentration increases to a predetermined level. At this stage, the FPM controller 162 opens the auxiliary brine replacement control valve 140, closes the recirculation control valve 124 and opens the auxiliary feed water control valve 148. The concentrate collector brine 120 flows through the auxiliary brine replacement conduit 136 and the replacement control valve of
25 auxiliary brine 140 via auxiliary tank feed conduit 138 to auxiliary feed water tank 142. Auxiliary feed water tank 142 is filled with feedwater before opening of the brine replacement control valve auxiliary 140, as described below. The brine enters the auxiliary feed water tank 142 and conducts the feed water from the tank
30 142 towards the feed manifold 114 by the auxiliary feed water condiment 146 and the auxiliary feed water control valve 148. It is noted that the water in the auxiliary feed water tank 142 can be maintained at the same pressure as the brine, such as by keeping the auxiliary brine replacement control valve 140 in an open state as the water pressure
35 in the system increases gradually. Alternatively, the water in the auxiliary feed water tank 142 can be maintained at a pressure much lower than the brine pressure but higher than the atmospheric pressure by operating the auxiliary feed water pump 144, as described below.
During washing, the FPM controller 162 opens the recycle duct control valve 156, which produces a flow of water from a location downstream of the pump 102 to a location upstream of the pump 102, optionally through a restrictor 160, which decreases the feedwater pressure in the manifold 114 to a pressure greater than atmospheric pressure, which exceeds the osmotic pressure of the feedwater on the feed side of the module 100.
The concentrate flow sensor 130 measures the accumulated volume of brine flowing from the concentrate manifold 120 and, therefore, measures the cumulative volume of feed water entering the feed manifold 114 through the auxiliary feed water conduit 146 and auxiliary feed water control valve 148, which replaces the brine in module 100.
After total replacement of the brine with feedwater in module 100, the FPM controller 162 reopens the recirculation control valve 124 and closes the auxiliary brine replacement control valve 140, the feedwater control valve auxiliary 148 and the recycle duct control valve 156, providing a liquid flow, as shown in Figure 3C, which may be identical to the liquid flow illustrated in Figure 3A, in which the operation of the circulation pump 126 and high pressure pump 102 supplies mixed feed water to module 100.
Then, the FPM controller 162 periodically activates the auxiliary feed water pump 144 and opens the auxiliary brine outlet tank control valve 154 to wash the entire brine of the auxiliary feed water tank 142 through an outlet of auxiliary brine 152 to a location outside the at least one water treatment system, and to fill the auxiliary feed tank 142 with feed water for future replacement of the brine in module 100. This flow is shown in continuous black lines in Figure 3D.
After the total replacement of the brine with feed water in the auxiliary feed water tank 142, as measured by the auxiliary flow sensor 150, the FPM controller 162 closes the auxiliary brine outlet tank control valve 154 and the operation of the auxiliary feed water pump 144 ends.
Reference is now made to Figures 4A -4D, which are simplified illustrations of water flows in a second embodiment of the water treatment system of the type shown in Figure 1.
10 Before the start of the withdrawal of the concentrate from the module 100, the brine outlet control valve 134, the auxiliary brine replacement control valve 140, the auxiliary feed water control valve 148 and the control valve Recycling conduit 156 are closed and the recirculation control valve 124 is open. The concentrate of concentrate collector 120 is again directed towards the entrance of the collector of
Feed 114 via the recirculation conduit 122 and the recirculation control valve 124, as shown by an arrow with the CONCENTRATED label (Figure 1), which represents the recirculation flow in the recirculation conduit 122. In the feed manifold 114, the concentrate is mixed with the feedwater, as shown by means of an arrow with the MIXED label
20 (Figure 1), which represents the mixed flow in the feed manifold 114. Therefore, a mixed flow enters the pressure vessels 110 for further treatment. The water flow for this stage is shown in a continuous black line in Figure 4A.
Then, the feed pressure gradually increases as the salinity of the mixed water supplied to the membrane elements 112 increases, and the recirculation process described above continues.
Once the concentration of the concentrate reaches a threshold, such as a predetermined salinity level for which continuous water treatment is not considered
30 practicable, the FPM controller 162 opens the auxiliary brine replacement control valve 140, which is approximately at atmospheric pressure, which reduces the water pressure inside the module 100 to a pressure between the concentrate pressure in the module 100 and the feed water pressure in the auxiliary feed tank
142. 35
Immediately after, the FPM controller 162 closes the recirculation control valve 124 and opens the auxiliary feed water control valve 148. The feedwater of the auxiliary feed tank 142 flows through the auxiliary feed water conduit 146 and the feedwater control valve 148 towards the
5 feed manifold 114, as shown in Figure 48, thereby supplying feedwater to module 100 at a pressure greater than the osmotic pressure of the feedwater and slightly greater than the pressure necessary for osmosis to occur. inverse
10 The concentrate flow rate sensor 130 measures the accumulated volume of brine flowing from the concentrate manifold 120 and, therefore, measures the cumulative volume of feedwater entering the feed manifold 114 through the feedwater conduit auxiliary 146 and auxiliary feed water control valve 148, which replaces the brine in module 100.
15 After total replacement of the brine with feed water in module 100, the FPM controller 162 reopens the recirculation control valve 124 and closes the auxiliary brine replacement control valve 140 and the water control valve of auxiliary feed 148, providing a liquid flow, as shown in Figure
20 4C, which may be identical to the liquid flow illustrated in Figure 4A, in which the operation of the high pressure pump 102 and the circulation pump 126 supplies mixed feed water to the module 100.
Then, the FPM 162 controller periodically activates the feed water pump
25 auxiliary 144 and opens the auxiliary brine outlet tank control valve 154 to wash the entire brine of the auxiliary feed water tank 142 through an auxiliary brine outlet 152 to a location outside the at least one treatment system of water, and to fill the auxiliary feed tank 142 with feed water for the additional replacement of the brine in the module 100 with the water of
30 feed, as described above, as seen in Figure 4D. After the total replacement of the brine with feed water in the auxiliary feed water tank 142, as measured by the auxiliary flow sensor 150, the FPM controller 162 closes the auxiliary brine outlet tank control valve 154 and the operation of the auxiliary feed water pump 144 ends.
Reference is now made to Figures 5A-5C, which are simplified illustrations of water flows in another embodiment of the water treatment system of the type shown in Figure 1.
5 Before the start of the withdrawal of concentrate from module 100, the outlet control valvebrine 134, auxiliary brine replacement control valve 140, the valveauxiliary feed water control 148 and recycle duct control valve156 are closed and the recirculation control valve 124 is open. The concentrateof the concentrate manifold 120 is directed again towards the entrance of the collector of
10 supply 114 via the recirculation conduit 122 and the recirculation control valve 124, as shown by means of an arrow with the CONCENTRATED label (Figure 1), which represents the recirculation flow in the recirculation conduit 122. In the feed manifold 114, the concentrate is mixed with the feedwater, as shown by means of an arrow with the MIXED label
15 (Figure 1), which represents the mixed flow in the feed manifold 114. Therefore, a mixed flow enters the pressure vessels 110 for further treatment. The water flow for this stage is shown in a continuous black line in Figure 5A.
Then, the feed pressure gradually increases as the salinity of the mixed water supplied to the membrane elements 112 increases, and the recirculation process described above continues.
Once the concentration of concentrate reaches a threshold, such as a predetermined salinity level for which continuous water treatment is not considered
25 practicable, the FPM controller 162 closes the concentrate recirculation control valve 124 and opens, at least partially, the brine outlet control valve 134, allowing the brine to flow through the brine outlet 132 towards a location outside the at least one water treatment system, which reduces the system pressure to a pressure higher than atmospheric pressure, said pressure exceeds the
30 osmotic pressure of the feed water on the feed side of the module 100. The brine is washed thoroughly through the brine outlet 132 of the at least one water treatment system, as the high pressure feed pump 102 continues to pump allied feed water from module 100, as shown in Figure 58. It is possible to increase the flow of the pump 102 at this stage
35 to accelerate brine washing.
The concentrate flow sensor 130 measures the accumulated volume of brine flowing from the concentrate manifold 120 and, therefore, measures it when the total washing of the brine out of the module 100 has finished.
After thoroughly washing the brine of module 100, the FPM controller 162 reopens the recirculation control valve 124 and closes the brine outlet control valve 134, providing a liquid flow, as shown in Figure SC, which it may be identical to the liquid flow illustrated in Figure SA, in which the operation of the high pressure pump 102 and the circulation pump 126 supplies mixed feed water to the module 100.
Reference is now made to Figures 6A-60, which are simplified illustrations of water flows in yet another embodiment of the water treatment system of the type shown in Figure 1.
Prior to the start of the withdrawal of the concentrate from the module 100, the brine outlet control valve 134, the auxiliary brine replacement control valve 140, the auxiliary feed water control valve 148 and the duct control valve Recycling 156 are closed and the recirculation control valve 124 is open. The concentrate of the concentrate manifold 120 is again directed towards the entrance of the feed manifold 114 through the recirculation conduit 122 and the recirculation control valve 124, as shown by means of an arrow with the CONCENTRATE label (Figure 1) , which represents the recirculation flow in the recirculation duct 122. In the feed manifold 114, the concentrate is mixed with the feedwater, as shown by means of an arrow with the MIXED label (Figure 1), which represents the mixed flow in the feed manifold 114. Therefore, a mixed flow enters the pressure vessels 110 for further treatment. The water flow for this stage is shown in a continuous black line in Figure 6A.
Then, the feed pressure gradually increases as the salinity of the mixed liquid supplied to the membrane elements 112 increases, and the recirculation process described above continues.
Once the concentrate concentration reaches a threshold, such as a predetermined pressure level, the FPM controller 162 opens the auxiliary brine replacement control valve 140, closes the recirculation control valve 124 and opens the control valve of auxiliary feed water 148. Brine from concentrate manifold 120
5 flows through the auxiliary brine replacement conduit 136, the auxiliary brine replacement control valve 140 and the auxiliary tank feed line 138 towards the auxiliary feed water tank 142.
The auxiliary feed water tank 142 is filled with feedwater before
10 opening the brine replacement control valve 140, as described below. The brine entering the auxiliary feed water tank 142 conducts the feed water thereto to the feed manifold 114 through an auxiliary feed water conduit 146 and an auxiliary feed water control valve 148.
15 The water flow for this stage is shown in a continuous black line in Figure 6B.
It is noted that the water in the auxiliary feed water tank 142 can be maintained at a pressure that is generally that of the brine pressure, such as by maintaining the opening of the auxiliary brine replacement control valve 140 in a Open state as the water pressure in the system gradually increases. Alternatively, the water in the auxiliary feed water tank 142 can be maintained at a pressure much lower than the brine pressure but higher than the atmospheric pressure by operating the feed water pump
Auxiliary 144, as described below.
In the embodiment of Figures 6A-6D, the FPM controller 162 increases the flow rate of the circulation pump 126 during washing to achieve a faster replacement of the brine of the module 100 with feedwater from the auxiliary feed tank 142,
30 therefore, the time necessary for the brine to be washed from module 100 and replaced by the feed water is reduced. A typical graph of the flow as a function of time, as measured by the concentrate flow sensor 130, located downstream of the circulation pump 126, appears in an enlarged part of Figure 6B, in which line 200 represents the flow as a function of time.
The concentrate flow sensor 130 measures the accumulated volume of brine flowing from the concentrate manifold 120 and, therefore, measures the cumulative volume of feed water entering the feed manifold 114 through the auxiliary feed water conduit 146 and auxiliary feed water control valve 148, which replaces the brine in module 100.
After the total replacement of the brine with feedwater in module 100, the FPM controller 162 reopens the recirculation control valve 124, closes the auxiliary brine replacement control valve 140 and the feedwater control valve auxiliary 148 and reduces the flow of the circulation valve 126 to the flow rate before opening the concentrate recirculation control valve 124, providing a liquid flow, as shown in Figure 6G, which may be identical to the illustrated liquid flow in Figure 6A, in which the operation of the high pressure pump 102 and the circulation pump 126 supplies mixed feed water to the module 100.
Then, the FPM controller 162 periodically activates the auxiliary feed water pump 144 and opens the auxiliary brine outlet tank control valve 154 to wash the entire brine of the auxiliary feed water tank 142 through an outlet of auxiliary brine 152 to a location outside the at least one water treatment system, and to fill the auxiliary feed tank 142 with feed water for additional replacement of the brine in module 100 with the feed water, as described above, as seen in Figure 60.
After the total replacement of the brine with feed water in the auxiliary feed water tank 142, as measured by the auxiliary flow sensor 150, the FPM controller 162 closes the auxiliary brine outlet tank control valve 154 and the operation of the auxiliary feed water pump 144 ends.
Again with reference to Figure 28, in which the periodic variations in the feedwater pressure during the water treatment correspond to the periodic variations in the salinity of the feedwater entering the module 100, as can be measured by a conductivity sensor (not shown), usually located downstream of pressure sensor 108. As in Figure 2A described above, the y-axis represents pressure variations in seawater desalination, and the x-axis
It represents time. The vertical line "A" represents the time at which a threshold is reached, such as a maximum feed water pressure threshold.
When the threshold is reached, the pressure vessels 110 are still filled with
5 concentrate, and mixed osmotic pressure and mixed feed water pressurecontinue to increase, until the feedwater enters the pressure vessels110 replacing the concentrate in these. Usually, when the threshold is reached, thesystem begins the brine washing process.
10 As described above, the osmotic pressure line of mixed feed water 170 represents the estimated osmotic pressure of the mixed feed water at the inlet of the module 100. Therefore, when the feed water of the pump 102 is mixed with the concentrate of the recirculation duct 122, the mixed osmotic pressure gradually increases, as observed in the gradual slope of the line 170. A
Once a threshold is reached, such as a salinity threshold or a pressure threshold, controller 162 begins the washing process. During the washing process, the concentrate is not recirculated back to the feed manifold 114, therefore, only the feedwater enters the feed manifold 114 and the mixed osmotic pressure decreases rapidly, as shown in the steep decrease in the
20 line 170.
Line 175 in Figure 28 illustrates the behavior of mixed feed water pressure in the prior art, represented by the teachings of U.S. Patent No. 8,025,804. Line 180 illustrates the pressure controlled by the controller so that it
25 maintain the delta pressure necessary for the desalination process by reverse osmosis not only during the gradual increase in the pressure of mixed feed water, when the concentrate is recirculated back to the feed manifold 114, but also when the brine is washed in the pressure vessels 110 by feeding feed water alone without recirculated concentrate. As it
30 observes in Figure 28, the increase in the flow of the circulation pump 126, compared to the flow of the circulation pump 126 used in the example of Figure 2A, causes the mixed osmotic pressure line 170, as well as the mixed feed water pressure line 180, decrease even more rapidly than in the example shown in Figure 2A. In Figure 28, the increase in the difference between line 175 and
35 line 180, compared to the difference between the two lines in Figure 2A, illustrates a greater benefit of operation at lower pressures when the flow rate is increased, thereby saving additional energy beyond the additional energy necessary for the Circulation pump 126 run at a higher flow rate.
5 Reference is now made to Figures 7A -70, which are simplified illustrationsof water flows in a further embodiment of the type water treatment systemshown in Figure 1.
Before the start of the withdrawal of concentrate from module 100, the outlet control valve
10 brine 134, the auxiliary brine replacement control valve 140, the auxiliary feed water control valve 148 and the recycle duct control valve 156 are closed and the recirculation control valve 124 is open. The concentrate of the concentrate manifold 120 is again directed towards the inlet of the feed manifold 114 via the recirculation conduit 122 and the control valve of
15 recirculation 124, as shown by means of an arrow labeled CONCENTRATE (Figure 1), which represents the recirculation flow in the recirculation duct 122. In the feed manifold 114, the concentrate is mixed with the water of feed, as shown by means of an arrow labeled MIXED (Figure 1), which represents the mixed flow in the feed conduit 114. Therefore, a
20 mixed flow enters the pressure vessels 110 for further treatment. The water flow for this stage is shown in a continuous black line in Figure 7 A.
Then, the feed pressure gradually increases as the salinity of the mixed water supplied to the membrane elements 112 increases, and the recirculation process described above continues.
Once the concentrate concentration reaches a threshold, such as a predetermined salinity level for which the continuous water treatment is deemed not practicable, the FPM controller 162 opens the 30 auxiliary brine replacement control valve 140 , close the recirculation control valve 124 and open the auxiliary feed water control valve 148. The FPM controller also increases the flow rate produced by the circulation pump 126. The brine from the concentrate manifold 120 flows through the conduit of auxiliary brine replacement 136, auxiliary tank feed conduit 138 and auxiliary brine replacement control valve 35 140 towards auxiliary feed water tank 142. Auxiliary feed water tank 142 is filled with water from supply before opening the auxiliary brine replacement control valve 140, as described below. The brine enters the auxiliary feed water tank 142 and conducts the feed water from the tank 142 to the feed manifold 114 through the 5 auxiliary feed water conduit 146 and the auxiliary feed water control valve 148. It Note that the water in the auxiliary feed water tank 142 may be at the same pressure as the brine pressure, such as by maintaining the auxiliary brine replacement control valve 140 in an open state as the pressure of the Water in the system gradually increases. By way of
10 Alternatively, the water in the auxiliary feed water tank 142 can be maintained at a pressure much lower than the brine pressure but higher than the atmospheric pressure by operating the auxiliary feed water pump 144, as described then.
In this embodiment, during washing, the FPM controller 162 opens the recycle duct control valve 156, which produces a flow of water from a location downstream of the pump 102 to a location upstream of the pump 102 , through a restrictor 160, which decreases the supply water pressure in the manifold 114 to a pressure greater than atmospheric pressure, said pressure exceeds the osmotic pressure of the
20 feed water on the feed side of module 100. The water flow for this stage is shown in a continuous black line in Figure 7B.
A typical graph of the flow as a function of time, as measured by the concentrate flow sensor 130, located downstream of the circulation pump 126, 25 appears in an enlarged part of Figure 7B, in which line 200 represents the flow as a function of time.
The concentrate flow sensor 130 measures the accumulated volume of brine flowing from the concentrate manifold 120 and, therefore, measures the accumulated volume of water
30 that enters the feed manifold 114 through the auxiliary feed water line 146 and the auxiliary feed water control valve 148, which replaces the brine in module 100. After the total replacement of the brine with water from In the module 100, the FPM controller 162 reopens the recirculation control valve 124 and closes the valve
35 auxiliary brine replacement control 140, auxiliary feed water control valve 148 and recycle duct control valve 156, providing a liquid flow, as shown in Figure 7e, which may be identical to liquid flow illustrated in Figure 7 A, in which the operation of the high pressure pump 102 and the circulation pump 126 supplies mixed feed water to the module 100.
Then, the FPM controller 162 periodically activates the auxiliary feed water pump 144 and opens the auxiliary brine outlet tank control valve 154 to wash the entire brine of the auxiliary feed water tank 142 through an outlet of auxiliary brine 152 to a location outside the at least one water treatment system, and to fill the auxiliary feed tank 142 with feed water for additional replacement of the brine in module 100. This flow is shown in continuous black lines in Figure 70.
After the total replacement of the brine with feed water in the auxiliary feed water tank 142, as measured by the auxiliary flow sensor 150, the FPM controller 162 closes the auxiliary brine outlet tank control valve 154 and the operation of the auxiliary feed water pump 144 ends.
Reference is now made to Figures 8A-8D, which are simplified illustrations of water flows in yet another embodiment of the water treatment system of the type shown in Figure 1.
Prior to the start of the withdrawal of the concentrate from the module 100, the brine outlet control valve 134, the auxiliary brine replacement control valve 140, the auxiliary feed water control valve 148 and the duct control valve Recycling 156 are closed and the recirculation control valve 124 is open. The concentrate of the concentrate manifold 120 is again directed towards the entrance of the feed manifold 114 through the recirculation conduit 122 and the recirculation control valve 124, as shown by means of an arrow with the CONCENTRATE label (Figure 1) , which represents the recirculation flow in the recirculation duct 122. In the feed manifold 114, the concentrate is mixed with the feedwater, as shown by means of an arrow with the MIXED label (Figure 1), which represents the mixed flow in the feed manifold 114. Therefore, a
mixed flow enters the pressure vessels 110 for further treatment. The water flow for this stage is shown in a continuous black line in Figure 8A.
Then, the feed pressure gradually increases as the salinity of the mixed water supplied to the membrane elements 112 increases, and the recirculation process described above continues.
Once the concentration of the concentrate reaches a threshold, such as a predetermined salinity level for which the continuous water treatment is not considered practicable, the FPM controller 162 opens the auxiliary brine replacement control valve 140, which It is approximately at atmospheric pressure, which reduces the water pressure inside module 100 to a pressure between the concentrate pressure in module 100 and the feed water pressure in the auxiliary feed tank
142.
15 Immediately thereafter, the FPM controller 162 closes the recirculation control valve 124 and opens the auxiliary feed water control valve 148. The feedwater of the auxiliary feed tank 142 flows through the auxiliary feed water conduit 146 and the feedwater control valve 144 towards the
20 feed manifold 114, as shown in Figure 88, thereby supplying feedwater to module 100 at a pressure greater than the osmotic pressure of the feedwater and slightly greater than the pressure necessary for osmosis to occur. inverse
In the embodiment illustrated in Figures 8A-8D, the FPM controller 162 also increases the flow rate of the circulation pump 126 during washing to achieve a faster replacement of the brine of the module 100 with feed water from the feed tank. Auxiliary 142, therefore, reduces the time required for the brine to be washed from the module 100 and replaced by the feed water. A typical graphic of
30 flow rate as a function of time, as measured by the concentrate flow sensor 130, located downstream of the circulation pump 126, appears in an enlarged part of Figure 88, in which line 200 represents the flow rate at time function. The water flow for this stage is shown in a continuous black line in Figure 88.
The concentrate flow sensor 130 measures the accumulated volume of brine flowing from the concentrate manifold 120 and, therefore, measures the cumulative volume of feed water entering the feed manifold 114 through the auxiliary feed water conduit 146 and auxiliary feed water control valve 148, which
5 replace the brine in module 100.
After the total replacement of the brine with feedwater in module 100, the FPM controller 162 reopens the recirculation control valve 124, closes the auxiliary brine replacement control valve 140 and the feedwater control valve 10 auxiliary 148 and reduces the flow of the circulation valve 126 to the flow rate before opening the concentrate recirculation control valve 124, providing a liquid flow, as shown in continuous black lines in Figure BC, which can be identical to the liquid flow illustrated in Figure BA, in which the operation of the high pressure pump 102 and the circulation pump 126 supplies mixed feed water to the
15 module 100.
Then, the FPM controller 162 periodically activates the auxiliary feed water pump 144 and opens the auxiliary brine outlet tank control valve 154 to wash the entire brine of the auxiliary feed water tank 142 through a
20 auxiliary brine outlet 152 to a location outside the at least one water treatment system, and to fill the auxiliary feed tank 142 with feed water for additional replacement of the brine in module 100. This flow is shown in solid black lines in Figure 80.
25 After the total replacement of the brine with feed water in the auxiliary feed water tank 142, as measured by the auxiliary flow sensor 150, the FPM controller 162 closes the brine outlet tank control valve auxiliary 154 and the auxiliary feed water pump operation 144 ends.
30 Reference is now made to Figures 9A-90, which are simplified illustrations of the water flows in yet another embodiment of the water treatment system of the type shown in Figure 1. Before the start of the withdrawal of the concentrate of module 100, brine outlet control valve 134, auxiliary brine replacement control valve 140, valve
35 auxiliary feed water control 148 and recycle duct control valve
156 are closed and the recirculation control valve 124 is open. The concentrate of the concentrate manifold 120 is again directed towards the inlet of the feed manifold 114 through the recirculation conduit 122 and the recirculation control valve 124, as shown by means of an arrow with the label 5 CONCENTRATE (Figure 1 ), which represents the recirculation flow in the recirculation duct 122. In the feed manifold 114, the concentrate is mixed with the feedwater, as shown by means of an arrow with the MIXED label (Figure 1), which represents the mixed flow in the feed conduit 114. Therefore, a mixed flow enters the pressure vessels 110 for further treatment. Water flow
10 for this stage is shown in a continuous black line in Figure 9A.
Then, the feed pressure gradually increases as the salinity of the mixed water supplied to the membrane elements 112 increases, and the recirculation process described above continues.
Once the concentration of the concentrate reaches a threshold, such as a predetermined salinity level for which the continuous water treatment is not considered practicable, the FPM controller 162 opens, at least partially, the outlet control valve of brine 134, which allows brine to flow through the outlet of
Brine 132 towards a location outside the at least one water treatment system, which reduces the system pressure in module 100.
Additionally, in the embodiment shown in Figures 9A-9D, during washing, the FPM controller 162 opens the recycle duct control valve 156, which
25 which produces a flow of water from a location downstream of the pump 102 to a location upstream of the pump 102, through a restrictor 160, which maintains the feedwater pressure in the manifold 114 at a higher pressure at atmospheric pressure, said pressure exceeds the osmotic pressure of the feed water on the feed side of the module 100, as seen in Figure 98.
Immediately afterwards, the FPM controller also opens the auxiliary brine replacement control valve 140, closes the recirculation control valve 124 and opens the auxiliary feed water control valve 148. The concentrate collector brine 120 flows to through the auxiliary brine replacement conduit 136, the
35 auxiliary tank feed conduit 138 and replacement control valve
auxiliary brine 140 to auxiliary feed water tank 142. The auxiliary feed water tank 142 is filled with feed water before the opening of the auxiliary brine replacement control valve 140, as described below. The brine enters the auxiliary feed water tank 142 and conducts the feed water from the tank 142 to the feed manifold 114 through the auxiliary feed water conduit 146 and the auxiliary feed water control valve 148. It Note that the water in the auxiliary feed water tank 142 may be at the same pressure as the brine pressure, such as by maintaining the auxiliary brine replacement control valve 140 in an open state at 10 as the pressure of water in the system gradually increases. Alternatively, the water in the auxiliary feed water tank 142 can be maintained at a pressure much lower than the brine pressure but higher than the atmospheric pressure by operating the auxiliary feed water pump 144, as described in continuation. The water flow for this stage is shown in a black line
15 continues in Figure 98.
The concentrate flow sensor 130 measures the accumulated volume of brine flowing from the concentrate manifold 120 and, therefore, measures when the total washing of the brine of the module 100 has finished. After the total washing of the module brine 20 100, the FPM controller 162 reopens the recirculation control valve 124 and closes the brine outlet control valve 134, the auxiliary brine replacement control valve 140, the auxiliary feed water control valve 148 and the recycle duct control valve 156, providing a liquid flow, as shown in Figure ge, which may be identical to the liquid flow illustrated in Figure 9A, in which the
The operation of the high pressure pump 102 and the circulation pump 126 supplies mixed feed water to the module 100.
Then, the FPM controller 162 periodically activates the auxiliary feed water pump 144 and opens the auxiliary brine outlet tank control valve 154 for
30 wash all brine from auxiliary feed water tank 142 through an auxiliary brine outlet 152 to a location outside the at least one water treatment system, and to fill auxiliary feed tank 142 with feed water to the additional replacement of the brine in module 100. This flow is shown in solid black lines in Figure 90.
After the total replacement of the brine with feed water in the auxiliary feed water tank 142, as measured by the auxiliary flow sensor 150, the FPM controller 162 closes the auxiliary brine outlet tank control valve 154 and the operation of the auxiliary feed water pump 144 ends.
It is noted that in the embodiment shown in Figure 98, as described above, a portion of the brine exits through the brine outlet 132 and, therefore, is not replaced with water from the auxiliary feed water tank 142. The volume of water in module 100 can be refilled by increasing the pump flow rate to
10 pressure 102 or by any other suitable method.
Reference is now made to Figures 1DA -100, which are simplified illustrations of water flows in even another embodiment of the water treatment system of the type shown in Figure 1.
Prior to the start of the withdrawal of the concentrate from the module 100, the brine outlet control valve 134, the auxiliary brine replacement control valve 140, the auxiliary feed water control valve 148 and the duct control valve Recycling 156 are closed and the recirculation control valve 124 is open. The concentrate 20 of the concentrate manifold 120 is again directed towards the inlet of the feed manifold 114 through the recirculation conduit 122 and the recirculation control valve 124, as shown by means of an arrow with the CONCENTRATE label (Figure 1 ), which represents the recirculation flow in the recirculation duct 122. In the feed manifold 114, the concentrate is mixed with the water
25, as shown by means of an arrow labeled MIXED (Figure 1), which represents the mixed flow in the supply line 114. Therefore, the mixed flow enters the pressure vessels 110 for treatment additional. The water flow for this stage is shown in a continuous black line in Figure 10A.
30 Then, the feed pressure gradually increases as the salinity of the mixed water supplied to the membrane elements 112 increases, and the recirculation process described above continues. Once the concentration of the concentrate reaches a threshold, such as a predetermined salinity level for which continuous water treatment is not considered
35 practicable, the FPM controller 162 opens the auxiliary brine replacement control valve 140, which is approximately at atmospheric pressure, which reduces the water pressure within the module 100 to a pressure between the concentrate pressure in the module 100 and the feed water pressure in the auxiliary feed tank
142.
Immediately afterwards, the FPM controller 162 closes the recirculation control valve 124 and opens the auxiliary feed water control valve 148. The brine of the concentrate manifold 120 flows through the auxiliary brine replacement conduit 136, the conduit of auxiliary tank feed 138 and auxiliary brine replacement control valve 140 towards auxiliary feed water tank 142. Auxiliary feed water tank 142 is filled with feedwater prior to opening of the control valve Auxiliary Brine Replacement 140, as described below. The brine entering the auxiliary feed water tank 142 conducts the feed water thereto to the feed manifold 114 through the auxiliary feed water conduit 146 and the auxiliary feed water control valve 148. It is noted that the Water in the auxiliary feed water tank 142 can be maintained at a pressure that is generally the same as the brine pressure, such as by maintaining the auxiliary brine replacement control valve 140 in an open state as the pressure of water in the system gradually increases. Alternatively, the water in the auxiliary feed water tank 142 can be maintained at a pressure much lower than the brine pressure but higher than the atmospheric pressure by operating the auxiliary feed water pump 144, as described below.
Additionally, in the embodiment of Figures 10A-10D, during washing, the FPM controller 162 opens the recycle duct control valve 156, which produces a flow of water from a location downstream of the pump 102 towards a location upstream of the pump 102, through a restrictor 160, which decreases the feedwater pressure in the manifold 114 to a pressure greater than atmospheric pressure, said pressure exceeds the osmotic pressure of the feedwater in the feed side of the module 100. The concentrate flow sensor 130 measures the accumulated volume of brine flowing from the concentrate manifold 120 and, therefore, measures the cumulative volume of feed water entering the feed manifold 114 through the water conduit of
auxiliary supply 146 and auxiliary supply water control valve 148, which replaces the brine in module 100.
After the total replacement of the brine with feedwater in module 100, the
5 FPM controller 162 reopens recirculation control valve 124 and closes the valveauxiliary brine replacement control 140, the water control valveauxiliary power 148 and recycle duct control valve 156,providing a liquid flow, as shown in Figure 10C, which can beidentical to the liquid flow illustrated in Figure 10A, above.
Then, the FPM controller 162 periodically activates the auxiliary feed water pump 144 and opens the auxiliary brine outlet tank control valve 154 to wash the entire brine of the auxiliary feed water tank 142 through an outlet of auxiliary brine 152 to a location outside the at least one system
15 water treatment, and to fill the auxiliary feed tank 142 with feed water for additional replacement of the brine in module 100. This flow is shown in solid black lines in Figure 100.
After total replacement of the brine with feed water in the water tank
Auxiliary feed 20, as measured by the auxiliary flow sensor 150, the FPM controller 162 closes the auxiliary brine outlet tank control valve 154 and terminates the operation of the auxiliary feed water pump 144.
Reference is now made to Figures 11A -110, which are simplified illustrations of water flows in another water treatment system of the type shown in Figure 1.
Before the start of the withdrawal of the concentrate from the module 100, the brine outlet control valve 134, the auxiliary brine replacement control valve 140, the check valve
30 auxiliary feed water control 148 and the recycle duct control valve 156 are closed and the recirculation control valve 124 is open. The concentrate of the concentrate manifold 120 is again directed towards the inlet of the feed manifold 114 through the recirculation conduit 122 and the recirculation control valve 124, as shown by means of an arrow with the label
CONCENTRATE (Figure 1), which represents the recirculation flow in the recirculation duct 122. In the feed manifold 114, the concentrate is mixed with the feedwater, as shown by means of an arrow with the MIXED label (Figure 1), which represents the mixed flow in the feed conduit 114. Therefore, a mixed flow enters the pressure vessels 110 for further treatment. Water flow
5 for this stage is shown in a continuous black line in Figure 11 A.
Then, the feed pressure gradually increases as the salinity of the mixed water supplied to the membrane elements 112 increases, and the recirculation process described above continues.
10 Once the concentrate concentration reaches a threshold, such as a predetermined salinity level for which it is considered that continuous water treatment is not practicable, controller 162 opens the auxiliary brine replacement control valve 140, which is connected to auxiliary feed water tank 142 through the
15 auxiliary brine replacement conduit 136 and auxiliary tank feed conduit 138. In this embodiment, the water in the auxiliary feed water tank 142 is approximately at atmospheric pressure, therefore, the valve opening is opened. auxiliary brine replacement control 140 reduces the water pressure inside module 100 to a pressure between the concentrate pressure in module 100 and the
20 feed water pressure in auxiliary feed tank 142.
Immediately afterwards, the FPM controller 162 closes the recirculation control valve 124 and opens the auxiliary feed water control valve 148. The brine of the concentrate manifold 120 flows through the auxiliary brine replacement conduit 136, the auxiliary tank feed conduit 138 and auxiliary brine replacement control valve 140 towards auxiliary feed water tank 142. The auxiliary feed water tank 142 is filled with feed water before the valve opening is opened. auxiliary brine replacement control 140, as described below. Brine entering auxiliary feed tank 30 142 conducts feedwater from auxiliary feedwater tank 142 through auxiliary feedwater conduit 146 and auxiliary feedwater control valve 148 to feed manifold 114, thereby supplying feed water to the module 100 at a pressure greater than the osmotic pressure of the feed water and not much greater than the pressure necessary for
35 that reverse osmosis occurs.
In this embodiment, during washing, the FPM controller 162 also opens the recycle duct control valve 156, which produces a flow of water from a location downstream of the pump 102 to a location upstream of the pump 102 , through a restrictor 160, which decreases the feedwater pressure in the manifold 114 to a pressure greater than atmospheric pressure, said pressure exceeds the osmotic pressure of the feedwater on the feed side of the module 100. In This embodiment illustrated in Figures 11A-11 D, the FPM controller also increases the flow rate produced by the circulation pump 126 during washing to achieve a faster replacement of the brine of the module 100 with feed water from the auxiliary feed tank 142, therefore, the time required for the brine to be washed from module 100 and replaced by the feed water is reduced. A typical graph of the flow as a function of time, as measured by the concentrate flow sensor 130, located downstream of the circulation pump 126, appears in an enlarged part of Figure 11 B, in which line 200 represents the flow as a function of time.
The water flow for this stage is shown in a continuous black line in Figure 11 B The concentrate flow sensor 130 measures the accumulated volume of brine flowing from the concentrate manifold 120 and, therefore, measures the accumulated volume of feedwater entering the feed manifold 114 through the auxiliary feedwater conduit 146 and the auxiliary feedwater control valve 148, which replaces the brine in module 100.
After total replacement of the brine with feed water in module 100, the FPM controller 162 reopens the recirculation control valve 124, closes the auxiliary brine replacement control valve 140, the feed water control valve auxiliary 148 and the recycle duct control valve 156, and reduces the flow of the circulation pump 126 to the flow rate before opening the recirculation control valve 124, providing a liquid flow, as shown in continuous black lines in Figure 11 e, which may be identical to the liquid flow illustrated in Figure 11 A, in which the operation of the high pressure pump 102 and the circulation pump 126 supplies water to the module 100.
Then, the FPM controller 162 periodically activates the auxiliary feed water pump 144 and opens the auxiliary brine outlet tank control valve 154 to wash the entire brine of the auxiliary feed water tank 142 through an outlet of auxiliary brine 152 to a location outside the at least one system
5 water treatment, and to fill auxiliary feed tank 142 with water frompower for additional replacement of the brine in module 100. This flow isshown in a continuous black line in Figure 11 D.
After total replacement of the brine with feed water in the water tank
10 auxiliary supply 142, as measured by the auxiliary flow sensor 150, the FPM controller 162 closes the auxiliary brine outlet tank control valve 154 and terminates the operation of the auxiliary supply water pump 144.
Those skilled in the art will note that the present invention is not limited to what is
15 showed and specifically described hereinbefore. Instead, the scope of the invention includes combinations and sub-combinations of the features described and shown above, as well as modifications thereof that could occur to those who read the foregoing description and which are not found in the prior art.

权利要求:
Claims (20)
[1]
1. A liquid treatment method comprising the steps of: supplying feed liquid to be treated to at least one treatment module of
The liquid that employs at least one membrane, the at least one module has a liquid inlet on a feed side of the at least one membrane, a permeate outlet on a permeate side of the at least one membrane and an outlet of brine on one brine side of the at least one membrane; Y
monitor liquid pressure within the at least one treatment module of
10 and after a liquid pressure threshold is exceeded in the at least one liquid treatment module, which represents the excess of a salinity threshold in the liquid in it, reduce the liquid pressure in the at least a liquid treatment module at a level that exceeds the osmotic pressure of the liquid in the at least one liquid treatment module making changes in the liquid supply to the module.
[2]
2. A method according to claim 1, wherein said reduction of the liquid pressure in the at least one liquid treatment module is performed by at least one of the following operations, and a combination thereof:
open a liquid pressure reduction valve at the brine outlet;
20 increasing a liquid volume output of a circulation pump that removes the brine from at least one liquid treatment module and supplies liquid to the liquid inlet at times other than when it is exceeded and immediately after this; balancing liquid pressures between a liquid pressure within the at least one liquid treatment module and within a liquid feed tank; Y
25 opening a recycle duct control valve in the liquid inlet, thereby providing a return flow liquid passage that reduces the pressure from the liquid inlet of the at least one liquid treatment module that avoids a pump High pressure upstream of the liquid inlet.
A method according to claim 1 or 2, further comprising the steps of:
circulating a concentrate from said brine outlet to said liquid inlet through said circulation pump and through a recirculation control valve disposed between said brine outlet and said liquid inlet; Y
After the liquid pressure threshold is exceeded, close the recirculation control valve.
[4]
4. A method according to any one of claims 1 to 3, comprising
5 further that said step of supplying the feed liquid to be treated at least oneLiquid treatment module is performed together with pressurizing the feed liquidby using a pump that normally maintains a volume of liquid offixed output feed regardless of variations in liquid pressure in theoutput of the same, the energy consumption of the pump depends on the variations in the
10 liquid pressure at the outlet.
[5]
5. A method according to claim 4, wherein said liquid pressure monitoring within the at least one liquid treatment module is performed by monitoring the liquid pressure at the pump outlet.
[6]
6. A method according to any of the preceding claims, wherein said reduction of the liquid pressure in the at least one liquid treatment module is carried out by means of ·
remove brine from at least one liquid treatment module; Y
20 reduce, at an improved rate, the pressure of the liquid in the at least one liquid treatment module by at least one of the following operations and a combination thereof: opening a pressure reducing valve downstream of the pump high pressure ;
25 increase the volume output of the circulation pump from its volume output when it functions as a concentrate circulation pump to a larger volume output when it functions as a feed liquid pump; Y
pass the liquid from downstream of the high pressure feed pump 30 upstream of the high pressure feed pump.
[7]
7. A method according to claim 6, wherein said passage of the liquid from downstream of the high pressure feed pump upstream of the high pressure feed pump includes passing the liquid through a water reducer.
35 flow arranged in parallel to the high pressure feed pump.
[8]
8. A method of liquid treatment comprising:
supplying liquid to be treated to at least one liquid treatment module that includes at least one membrane and that has a liquid inlet on a feed side of the at least one membrane, a permeate outlet on a side of
5 permeate of the at least one membrane and a brine outlet on a brine side of the at least one membrane;
pressurize the feed liquid supplied to the liquid inlet by using a pump that normally maintains a fixed output feed volume regardless of variations in the liquid pressure at the outlet of the
10 same, the energy consumption of the pump depends on the variations in the liquid pressure at the outlet,
monitor the liquid pressure at the pump outlet and when a predetermined high pressure threshold is reached at the pump outlet, make changes immediately in the liquid supply to the module, thereby causing the
15 Immediately decrease the liquid pressure at the pump outlet, to a pressure lower than the osmotic pressure on the supply side of a part but not of the entire module, thereby immediately reducing the energy consumption of the pump .
[9]
9. A method according to claim 8, wherein the liquid pressure in the
The pump outlet is reduced so that the liquid pressure in the at least one liquid treatment module exceeds the osmotic pressure of the liquid in the at least one liquid treatment module.
[10]
10. A method according to claim 8 or 9, wherein said reduction of the liquid pressure at the pump outlet is performed by at least one of the following
operations, and a combination thereof: open a liquid pressure reduction valve at the brine outlet; increase a liquid volume output of a circulation pump that removes the
brine the at least one liquid treatment module and supply liquid to the liquid inlet 30 at times other than when it is exceeded and immediately after this; balancing liquid pressures between a liquid pressure within the at least one liquid treatment module and within a liquid feed tank; Y
opening a recycle duct control valve in the liquid inlet, thereby providing a return flow liquid passage that reduces the pressure 35 from the liquid inlet of the at least one liquid treatment module that prevents a
high pressure pump upstream of the liquid inlet.
[11 ]
eleven . A method according to any of claims 8 to 10, wherein said reduction of the liquid pressure at the pump outlet is performed by: removing brine from at least one liquid treatment module; Y
5 reduce, at an improved rate, the pressure of the liquid in the at least one liquid treatment module by at least one of the following operations and a combination thereof:
open a pressure reducing valve downstream of the high pressure pump;
10 increase the volume output of the circulation pump from its volume output when it functions as a concentrate circulation pump to a larger volume output when it functions as a feed liquid pump; Y
pass the liquid from downstream of the high pressure feed pump 15 upstream of the high pressure feed pump.
[12]
12. A method according to claim 11, wherein said passage of the liquid from downstream of the high pressure feed pump upstream of the high pressure feed pump includes passing the liquid through a water reducer.
20 flow arranged in parallel to the high pressure feed pump.
[13]
13. A method according to any of claims 8 to 12, further comprising the steps of: circulating a concentrate from said brine outlet to said liquid inlet by said circulation pump and by a recirculation control valve disposed between said brine outlet and said liquid inlet; Y
After the liquid pressure threshold is exceeded, close the recirculation control valve.
A water treatment system comprising: at least one liquid treatment module that employs at least one membrane, the at least one module has a liquid inlet on a feed side of the at least one membrane, a permeate outlet on one permeate side of the at least one membrane and one brine outlet on one side of
35 brine of the at least one membrane; a high pressure pump, operative to pressurize the liquid to be treated
received at a liquid feed inlet; a circulation pump to circulate the concentrated brine outlet to said liquid inlet; and a system controller configured to receive an output indication of
5 the liquid pressure within the at least one liquid treatment module and after a threshold of the liquid pressure is exceeded in the at least one liquid treatment module, which represents the excess of a salinity threshold in the liquid in this, reduce the pressure of the liquid in the at least one liquid treatment module to a level that exceeds the osmotic pressure of the
10 liquid in the at least one liquid treatment module making changes in the liquid supply to the module.
[15]
15. A system according to claim 14, further comprising: a liquid pressure reducing valve at the brine outlet; a feed tank of
15 liquid in communication with the brine outlet; and a recycle duct control valve in the liquid inlet; wherein the reduction of the liquid pressure in the at least one liquid treatment module is performed under the control of said system controller by at least one of the following operations, and a combination thereof:
20 opening said liquid pressure reducing valve; increase a liquid volume output from the circulation pump; balance liquid pressures between a liquid pressure within the at least one
liquid treatment module and within said liquid feed tank; and opening said recycle duct control valve, thereby providing
25 a return flow liquid passage that reduces the pressure from the liquid inlet of the at least one liquid treatment module that avoids the high pressure pump upstream of the liquid inlet.
[16]
16. A system according to claim 14 or 15, further comprising a
30 recirculation control valve disposed between said brine outlet and said liquid inlet, in which said circulation of the concentrate is performed by the recirculation control valve, after the liquid pressure threshold is exceeded, the flow controller system is configured to close the recirculation control valve.
35 17.A system according to any of claims 14 to 16, wherein
bliss high pressure pumpbeset upforkeep normallyavolumefrom
fifty
Fixed output feed liquid regardless of variations in the liquid pressure at the outlet thereof, the energy consumption of the pump depends on the variations in the liquid pressure at the outlet.
A system according to claim 17, further comprising a pressure sensor disposed at said pump outlet, for monitoring the liquid pressure within the at least one liquid treatment module.
[19]
19. A system according to any of claims 14 to 18, wherein said reduction of the liquid pressure in the at least one liquid treatment module
is performed by: removing brine from at least one liquid treatment module; and reduce, at an improved rate, the pressure of the liquid in the at least one module of
liquid treatment by at least one of the following operations and a combination thereof: open a pressure reducing valve downstream of the high pressure pump;
increase the volume output of the circulation pump from its volume output when it functions as a concentrate circulation pump to a larger volume output when it functions as a liquid pump
feeding; and passing the liquid from downstream of the high pressure feed pump to upstream of the high pressure feed pump.
A system according to claim 19, further comprising a flow restrictor arranged in parallel to the high pressure feed pump; and wherein said passage of the liquid from downstream of the high pressure feed pump upstream of the high pressure feed pump includes passing the liquid through said flow reducer.
[21 ]
twenty-one . A liquid treatment system comprising:
at least one liquid treatment module that employs at least one membrane, the at least one module has a liquid inlet on a feed side of the at least one membrane, a permeate outlet on a side of
Permeate of the at least one membrane and a brine outlet on a brine side of the at least one membrane;
a high pressure pump, operative to pressurize liquid to be treated received at a liquid feed inlet and configured to normally maintain a fixed output feed volume regardless of variations in the liquid pressure at the outlet thereof, the energy consumption
5 of the pump depends on the variations in the liquid pressure at the outlet; a circulation pump to circulate the concentrated brine outlet to said liquid inlet; and a system controller configured to receive an output indication of the liquid pressure at the pump outlet and when a threshold of
10 predetermined high pressure at the pump outlet, make changes immediately in the liquid supply to the module, thereby causing the immediate decrease of the liquid pressure at the pump outlet, to a pressure lower than the osmotic pressure on the power side of a part but not all of the module, thereby immediately reducing energy consumption
15 of the pump.
[22]
22. A system according to claim 21, wherein the liquid pressure at the pump outlet is reduced such that the liquid pressure in the at least one liquid treatment module exceeds the osmotic pressure of the liquid in the at least one module
20 liquid treatment.
[23]
23. A system according to claim 21 or 22, further comprising: a liquid pressure reducing valve at the brine outlet; a liquid feed tank in communication with the brine outlet; and a control valve
25 of recycling duct in the liquid inlet; wherein the reduction of the liquid pressure in the at least one liquid treatment module is carried out under the control of said system controller by at least one of the following operations, and a combination thereof: opening said valve of liquid pressure reduction;
30 increase a liquid volume output from the circulation pump; balancing liquid pressures between a liquid pressure within the at least one liquid treatment module and within said liquid feed tank; Y
opening said recycle duct control valve, thereby providing a return flow liquid passage that reduces the pressure from the liquid inlet of the at least one liquid treatment module that avoids the pump from
high pressure upstream of the liquid inlet.
[24]
24. A system according to any of claims 21 to 23, wherein said reduction of the liquid pressure in the at least one liquid treatment module
5 is performed by: removing brine from at least one liquid treatment module; and reduce, at an improved rate, the pressure of the liquid in the at least one module of
liquid treatment by at least one of the following operations and a combination thereof: 10 open a pressure reducing valve downstream of the high pressure pump;
increase the volume output of the circulation pump from its output
volume when it functions as a concentrate circulation pump up to a
larger volume output when it functions as a liquid pump
15 feeding; and passing the liquid from downstream of the high pressure feed pump to upstream of the high pressure feed pump.
[25]
25. A system according to claim 24, further comprising a restrictor
20 of flow arranged in parallel to the high pressure feed pump; and wherein said passage of the liquid from downstream of the high pressure feed pump upstream of the high pressure feed pump includes passing the liquid through said flow reducer.
A system according to any one of claims 21 to 25, further comprising a recirculation control valve disposed between said brine outlet and said liquid inlet; wherein said circulation of the concentrate is performed by the recirculation control valve, after the liquid pressure threshold is exceeded, the system controller is configured to close the control valve of
30 recirculation.

类似技术:

---

公开号 | 公开日 | 专利标题

---

ES2673945A2|2018-06-26|System and method for water treatment

---

JP2009148673A|2009-07-09|Membrane separation apparatus and desalination method

---

KR101011403B1|2011-01-28|Forward osmotic membrane module and forward osmotic desalination device for using forward osmotic membrane modul and the method thereof

---

US20180280888A1|2018-10-04|Reverse osmosis treatment apparatus and reverse osmosis treatment method

---

KR102180787B1|2020-11-23|Water treatment system and method by reverse osmosis or nanofiltration

---

KR20180026541A|2018-03-12|Water purification system and method

---

JP2008307522A|2008-12-25|Desalting method, desalting apparatus, and bubble generator

---

JP4996067B2|2012-08-08|Water treatment apparatus using reverse osmosis membrane and method of using the same

---

KR101752553B1|2017-07-12|FO-RO hybrid system with double circulation type and control method of thereof

---

KR101802600B1|2017-11-28|water purifying system and backwash module control method thereof

---

KR101578470B1|2015-12-17|Closed circuit desalination retrofit unit for improved performance of common reverse osmosis systems

---

KR101516058B1|2015-04-30|Reverse osmosis membrane module-specific pressure controlled osmotic backwash system

---

JP2018519158A|2018-07-19|Method for controlling a desalination plant powered by a renewable energy source and associated plant

---

FI125584B|2015-12-15|A method for providing fluid circulation in membrane filtration and membrane filtration apparatus

---

JP6398132B2|2018-10-03|Water treatment apparatus and operation method thereof

---

JP5865714B2|2016-02-17|Seawater desalination equipment

---

KR101649741B1|2016-08-22|an apparatus for concentrating sap

---

KR101776046B1|2017-09-19|The method for operation of ballast treatment system

---

JP6033118B2|2016-11-30|Reverse osmosis membrane device

---

KR20130025801A|2013-03-12|Water purifier

---

JP6398131B2|2018-10-03|Water treatment apparatus and operation method thereof

---

WO2012145787A1|2012-11-01|Apparatus and method for reducing fouling and scaling in a fluid treatment system

---

KR20210039474A|2021-04-09|Large recovery variable volume reverse osmosis membrane system

---

KR101331842B1|2013-11-22|Sterilizing method for water tank of water purifier and sterilizing water purifier applied thereof

---

KR101558942B1|2015-10-08|an apparatus for concentrating sap

同族专利:

---

公开号 | 公开日

---

WO2016139672A4|2016-11-10|

---

US10435306B2|2019-10-08|

---

WO2016139672A1|2016-09-09|

---

IL254014D0|2017-10-31|

---

ES2673945R1|2018-09-11|

---

ES2673945B2|2019-05-29|

---

PE20180148A1|2018-01-18|

---

US20190144302A1|2019-05-16|

---

SG11201706954WA|2017-09-28|

---

CL2017002217A1|2018-04-13|

---

IL254014A|2020-07-30|

---

US20160257576A1|2016-09-08|

---

US10214430B2|2019-02-26|

---

MX2017011254A|2018-05-07|

引用文献:

---

公开号 | 申请日 | 公开日 | 申请人 | 专利标题

---

---

US3853756A|1973-02-12|1974-12-10|Westinghouse Electric Corp|Reverse pressure cleaning of supported semipermeable membranes|

---

US4169789A|1978-06-01|1979-10-02|Permo Sa|Process and apparatus for purifying sea water by reverse osmosis|

---

US4629568A|1983-09-26|1986-12-16|Kinetico, Inc.|Fluid treatment system|

---

US4814086A|1985-10-03|1989-03-21|Bratt Russell I|Method and apparatus for fluid treatment by reverse osmosis|

---

WO1988001529A1|1986-09-04|1988-03-10|Memtec Limited|Cleaning of hollow fibre filters|

---

HU200563B|1987-03-06|1990-07-28|Laszlo Szuecs|Method and apparatus for treating liquids consist of foreign matter by diaphragm filter device|

---

US4784771A|1987-08-03|1988-11-15|Environmental Water Technology, Inc.|Method and apparatus for purifying fluids|

---

DE4218115A1|1992-06-02|1993-12-09|Guenter Lauer|Process and treatment device for pure water production|

---

US5888401A|1996-09-16|1999-03-30|Union Camp Corporation|Method and apparatus for reducing membrane fouling|

---

IL157581A|2003-01-09|2004-08-31|Ide Technologies Ltd|Direct osmosis membrane cleaning|

---

IL157430A|2003-08-17|2009-08-03|Avi Efraty|Apparatus for continuous closed circuit desalination under variable pressure with a single container|

---

US7306735B2|2003-09-12|2007-12-11|General Electric Company|Process for the removal of contaminants from water|

---

NL1025459C2|2004-02-11|2005-08-12|Friesland Brands Bv|Device and method for micro or ultra filtration.|

---

WO2005123232A2|2004-06-21|2005-12-29|Membrane Recovery Ltd|Ro membrane cleaning method|

---

IL162713A|2004-06-24|2011-04-28|Desalitech Ltd|Apparatus and methods for continuous desalination in closed circuit without containers|

---

IL169654A|2005-07-13|2012-01-31|Desalitech Ltd|Continuous membrane filter separation of suspended particles in closed circuit|

---

JP4831480B2|2006-06-21|2011-12-07|三浦工業株式会社|Membrane filtration system|

---

US8025804B2|2006-12-19|2011-09-27|Avi Efraty|Continuous closed-circuit desalination method without containers|

---

DK2641652T3|2007-09-12|2019-04-29|Danisco Us Inc|FILTERING WITH INTERNAL POLLUTION CONTROL|

---

FR2933969B1|2008-07-21|2011-11-11|Degremont|INSTALLATION OF WATER DESALINATION BY REVERSE OSMOSIS|

---

JP5085675B2|2010-03-12|2012-11-28|株式会社東芝|Seawater desalination system|

---

US20140061129A1|2012-09-04|2014-03-06|Israel Aerospace Industries Ltd.|System and method of desalination of water|IL247687A|2016-09-07|2018-06-28|Israel Aerospace Ind Ltd|Method and system for liquid treatment|

---

EP3580180A4|2017-02-09|2021-01-06|Robert A. Bergstrom|Brine dispersal system|

---

US10882760B1|2020-05-13|2021-01-05|Benjamin John Koppenhoefer|System and method for reducing water pump cycling and TDS creep when producing purified water|

法律状态:
2018-06-26| BA2A| Patent application published|Ref document number: 2673945 Country of ref document: ES Kind code of ref document: A2 Effective date: 20180626 |

---

2018-09-11| EC2A| Search report published|Ref document number: 2673945 Country of ref document: ES Kind code of ref document: R1 Effective date: 20180904 |

---

2019-05-29| FG2A| Definitive protection|Ref document number: 2673945 Country of ref document: ES Kind code of ref document: B2 Effective date: 20190529 |

优先权:

---

申请号 | 申请日 | 专利标题

---

US14/638550|2015-03-04|

---

US14/638,550|US10214430B2|2015-03-04|2015-03-04|Water treatment system and method|

---

PCT/IL2016/050248|WO2016139672A1|2015-03-04|2016-03-03|System and method for water treatment|

---