DESC:FORM 2
THE PATENT ACT, 1970
(39 of 1970)
&
The Patent Rules, 2003
COMPLETE SPECIFICATION
(See section 10 and rule 13)
1. TITLE OF THE INVENTION:
A System and Method for Descaling Reverse Osmosis Membranes and to Achieve High Recovery Using Electrochemical / Two Stage Antiscalant Treated Reject Water
2. APPLICANT:
Name: WATERWALA LABS PVT LIMITED
Nationality: Indian
Address: #91A, 2nd Floor, Chukki Complex, 19th Main Rd, Sector 3, HSO Layout, Bengaluru, Karnataka – 560102.
3. PREAMBLE TO THE DESCRIPTION:
The following specification particularly describes the invention and the manner in which it is to be performed:

4. DESCRIPTION:
Field of the invention:
[0001]The present disclosure generally relates to the technical field of a RO water treatment system, and in specific relates to, a domestic RO system and method to achieve high recovery and to remove impurities such as chemical & biological contaminants and to produce a filtered concentrate effluent stream.
Background of the invention:
[0002]Highly purified water having a small concentration of ions and without any other contaminants is required for several industrial applications. For example, highly purified water must be used in the manufacture of electronic microchips: mineral contaminants can induce defects. Highly purified water is used in the power generation industry to minimize the formation of scale on the interior of pipes and thereby ensure good heat transfer within and unrestricted water flow through heat exchange systems.

[0003]The use of highly purified water reduces the formation of scale and deposits in water lines of heat exchange systems, thus extending the time interval between required maintenance procedures. The time interval between required maintenance procedures of a heat exchanging system should be as long as possible. Prolonging the time interval between required maintenance procedures is of particular importance in nuclear power systems, which require complex and expensive shutdown and start-up procedures and adherence to radiation safety protocols.

[0004]Several technical approaches towards water purification exist, including ion exchange resins. However, the need to periodically regenerate ion exchange resins requires a complex arrangement of pumps, piping, valves, and controls with associated large capital and maintenance costs and the use of regenerating chemicals which must be disposed of as chemical waste.

[0005]In existing technology, a concentrate recycle loop with a filtration module is known. Water purification systems include a concentrate filtration membrane and an electrode ionization unit. A concentrate effluent stream from the electrode ionization unit is filtered in the concentrate filtration membrane; the filtered concentrate effluent stream is provided to the concentrating compartments of the electrode ionization unit. However, the concentrate recycle loop with the filtration module does not efficiently purify the water.

[0006]Therefore, there is a need for a system that provide a system that is efficiently purifies the water. There is also a need for a system that removes impurities such as excess mineral & biological contaminants in the filtered concentrate effluent stream. There is also a need for a system that increases the recovery rate of RO systems and reduces water wastage from the RO purifiers. Further, there is also a need for a system that is easily installable and adaptable to existing RO purifiers so as to make accessible to a broader user base.
Objectives of the invention:
[0007]The primary objective of the invention is to provide a system and method to remove impurities such as excess mineral & biological foulants to produce a filtered concentrate effluent stream.

[0008]Another objective of the invention is to provide a system that increases the recovery rate of RO systems is increased to at least 53 %.

[0009]The other objective of the invention is to provide a system that reduces water wastage from the RO purifiers by at least 50%, thereby minimizing environmental impact and conserving precious water resources.

[0010]The other objective of the invention is to develop an efficient and cost-effective method for descaling RO membranes using an electrochemical / two stage antiscalant process, thereby reducing reliance on chemical additives and promoting responsible water management.

[0011]The other objective of the invention is to provide a system that is easily installable and adaptable to existing RO purifiers so as to make accessible to a broader user base.

[0012]The other objective of the invention is to provide a system that is cost-effective and energy-efficient solution that can be implemented widely for domestic RO water purification, offering economic and environmental benefits.

[0013]Yet another objective of the invention is to provide a system that utilizes the rejected high-TDS water from RO systems for further purification and reuse for non-potable purposes, maximizing water utilization and reducing drain water.

[0014]Further objective of the invention is to provide a system that prolongs the lifespan of RO membranes by preventing scaling and fouling through electro-descaling or two stage antiscalant based scale inhibition, minimizing maintenance and replacement costs.
Summary of the invention:
[0015]The present disclosure proposes a system and method for descaling reverse osmosis membranes and to achieve high recovery using electrochemical/two stage antiscalant treated reject water. The following presents a simplified summary in order to provide a basic understanding of some aspects of the claimed subject matter. This summary is not an extensive overview. It is not intended to identify key/critical elements or to delineate the scope of the claimed subject matter. Its sole purpose is to present some concepts in a simplified form as a prelude to the more detailed description that is presented later.

[0016]In order to overcome the above deficiencies of the prior art, the present disclosure is to solve the technical problem to provide a system and method to remove impurities such as chemical or biological contaminants to produce a filtered concentrate effluent stream.

[0017]According to an aspect, the invention provides a system for descaling reverse osmosis membranes using electrochemically / antiscalant treated reject water. In one embodiment herein, the system for descaling reverse osmosis membranes comprises a filtering unit, a first antiscalant unit, a pre-carbon filtration unit, a second antiscalant unit, a reverse osmosis (RO) filtration unit, a post-carbon filtration unit and a storage unit.

[0018]In one embodiment herein, the filtering unit is configured to receive wastewater through an inlet valve and remove sediments from the wastewater. In one embodiment herein, the first antiscalant unit is fluidly connected to the filtering unit via a solenoid valve and a pump. The first antiscalant unit is configured to receive the wastewater from the filtering unit and prevent a scale formation caused by dissolved salts, minerals, and hardness in the wastewater. The first antiscalant unit minimizes the scale formation due to the dissolved salts and minerals from the feed water via the control valve, thereby ensuring efficient separation and transfer of impurities.

[0019]In one embodiment herein, the pre-carbon filtration unit is fluidly connected to the first antiscalant unit. The pre-carbon filtration unit is configured to receive the feed water from the first antiscalant unit and remove one or more chemical contaminants in the wastewater. In particular, the one or more chemical contaminants include at least one of chlorine and organic impurities.

[0020]In one embodiment herein, the second antiscalant unit is fluidly connected to the pre-carbon filtration unit. The second antiscalant unit is configured to receive the wastewater from the pre-carbon filtration unit and prevent the dissolved salts and hardness minerals in the wastewater.

[0021]In one embodiment herein, the reverse osmosis (RO) filtration unit is fluidly connected to the second antiscalant unit. The RO filtration unit is configured to receive the reject water from the second antiscalant unit and remove salts, heavy metals, microorganisms and impurities in the reject water, thereby separating purified water and un-purified water from the wastewater. The un-purified water is transferred out from the RO filtration unit through a control valve.

[0022]In one embodiment herein, the post-carbon filtration unit is fluidly connected to the RO filtration unit. The post-carbon filtration unit is configured to receive the purified water from the RO filtration unit and remove residual odors or tastes in the purified water so as to improve water quality. In one embodiment herein, the storage unit is fluidly connected to the post-carbon filtration unit. The storage unit is configured to receive the purified water from the post-carbon filtration unit for usage. The storage unit comprises a disc member, and a micro switch.

[0023]In one embodiment herein, the disc member is configured to detect a flow level of the purified water in the storage unit, thereby transmitting a signal upon reaching a threshold value. In one embodiment herein, the micro switch is connected to the disc member. The micro switch is configured to receive the signal from the disc member, thereby activating the inlet valve to receive the wastewater into the filtering unit. The micro switch is configured to deactivate the inlet valve to restrict the wastewater into the filtering unit upon exceeding the threshold value of the purified water in the storage unit.

[0024]In one embodiment herein, the pump is configured to generate a pressure for transferring the wastewater from the solenoid valve to the first desalination unit. In one embodiment herein, the system comprises a flow sensor and a flow restricting member. In one embodiment herein, the flow sensor is positioned between the post-carbon filtration unit and the storage unit. The flow sensor is configured for measuring a flow rate to the purified water.

[0025]In one embodiment herein, the flow restricting member is positioned between the RO filtration unit and the control valve. The flow restricting member is configured for ensuring unidirectional flow of unpurified water while regulating pressure and preventing backflow.

[0026]According to another aspect, the invention provides a method for operating the system for descaling reverse osmosis membranes. At one step, the filtering unit receives the feed water through the inlet valve and removes sediments from the feed water. At another step, the first antiscalant unit receives the feed water from the filtering unit and partial recycled reject water and prevents a scale formation caused by dissolved salts, minerals and hardness in the feed water.

[0027]At another step, the pre-carbon filtration unit receives the feed water and partial recycled reject water from the first antiscalant unit and removing one or more chemical contaminants in the feed water. At another step, the second antiscalant unit receives the feed water from the pre-carbon filtration unit and prevents the scale formation due to excess minerals and hardness in the feed water and the partial recycled reject water.

[0028]At another step, the RO filtration unit receives the feed water and the partial recycled reject water from the second antiscalant unit and removes the minerals, heavy metals, microorganisms and other impurities in the feed water and the partial recycled reject water, thereby separating purified water and the un-purified water from the feed water and the partial recycled reject water. At another step, the post-carbon filtration unit receives the purified water from the RO filtration unit and removes residual chlorine, odors or tastes in the purified water so as to improve water quality. Further, at another step, the storage unit receives the purified water from the post-carbon filtration unit for usage.

[0029]Further, objects and advantages of the present invention will be apparent from a study of the following portion of the specification, the claims, and the attached drawings.
Detailed description of drawings:
[0030]The accompanying drawings, which are incorporated in and constitute a part of the specification, illustrate an embodiment of the invention, and, together with the description, explain the principles of the invention.

[0031]FIG. 1 illustrates a block diagram of a system for descaling reverse osmosis membranes, in accordance to an exemplary embodiment of the invention.

[0032]FIG. 2A illustrates a block diagram a basic configuration, in accordance to an example embodiment of the invention.

[0033]FIG. 2B illustrates a block diagram of an enhanced configuration with ESCS, in accordance to an example embodiment of the invention.

[0034]FIG. 2C illustrates a block diagram of an optimized configuration with two stage antiscalant, in accordance to an example embodiment of the invention.

[0035]FIG. 3 illustrates a block diagram of a reverse osmosis (RO) water filtration system, in accordance to an example embodiment of the invention.

[0036]FIG. 4 illustrates a block diagram of a high-recovery reverse osmosis (RO) water filtration system incorporating an Energy Saving Controller (ESC), in accordance to an example embodiment of the invention.

[0037]FIG. 5 illustrates a flowchart of a method for operating the system for descaling reverse osmosis membranes, in accordance to an exemplary embodiment of the invention.
Detailed invention disclosure:
[0038]Various embodiments of the present invention will be described in reference to the accompanying drawings. Wherever possible, same or similar reference numerals are used in the drawings and the description to refer to the same or like parts or steps.

[0039]The present disclosure has been made with a view towards solving the problem with the prior art described above, and it is an object of the present invention to provide a system and method to achieve high recovery by removing chemical & biological impurities to produce from the filtered concentrate effluent stream.

[0040]According to an embodiment of the invention, FIG.1 refers to a block diagram of a system 100 for descaling reverse osmosis membranes using two stage antiscalant treated reject water. In one embodiment herein, the system 100 for descaling reverse osmosis membranes comprises a filtering unit 102, a first antiscalant unit 106, a pre-carbon filtration unit 110, a second antiscalant unit 112, a reverse osmosis (RO) filtration unit 114, a post-carbon filtration unit 116, and a storage unit 118.

[0041]In one embodiment herein, the filtering unit 102 is configured to receive feed water through an inlet valve 104 and remove sediments from the feed water. In one embodiment herein, the first antiscalant unit 106 is fluidly connected to the filtering unit 102 via a solenoid valve 108 and a pump 124. The first antiscalant unit 106 is configured to receive the feed water from the filtering unit 102 and prevent a scale formation caused by dissolved salts, minerals, and hardness in the wastewater.

[0042]The first antiscalant unit 106 minimizes the scale formation due dissolved salts and minerals from the wastewater via the control valve 126, thereby ensuring efficient separation and transfer of impurities. The first desalination unit injects a controlled amount of an anti-scaling chemical to prevent calcium and magnesium deposition on the RO filtration unit.

[0043]In one embodiment herein, the pre-carbon filtration unit 110 is fluidly connected to the first antiscalant unit 106. The pre-carbon filtration unit 110 is configured to receive the wastewater from the first antiscalant unit 106 and remove one or more chemical contaminants in the wastewater. In particular, the one or more chemical contaminants include at least one of chlorine and organic impurities. The pre-carbon filtration unit 110 is composed of activated carbon block to efficiently adsorb chlorine, volatile organic compounds, and unpleasant odors.

[0044]In one embodiment herein, the second antiscalant unit 112 is fluidly connected to the pre-carbon filtration unit 110. The second antiscalant unit 112 is configured to receive the feed water from the pre-carbon filtration unit 110 and prevent the dissolved salts and hardness minerals in the feed water. The second antiscalant unit 112 is configured to provide additional scale prevention before the water reaches the RO filtration unit 114.

[0045]In one embodiment herein, the reverse osmosis (RO) filtration unit 114 is fluidly connected to the second antiscalant unit 112. The RO filtration unit 114 is configured to receive the wastewater from the second antiscalant unit 112 and minimizes the scale formation due to excess minerals and impurities in the wastewater, thereby separating purified water and un-purified water from the wastewater. The un-purified water is transferred out from the RO filtration unit 114 through a control valve 126.

[0046]In one embodiment herein, the post-carbon filtration unit 116 is fluidly connected to the RO filtration unit 114. The post-carbon filtration unit 116 is configured to receive the purified water from the RO filtration unit 114 and remove residual odors or tastes in the purified water so as to improve water quality. The post-carbon filtration unit 116 is configured to use coconut shell-activated carbon for enhancing the taste of purified water.

[0047]In one embodiment herein, the storage unit 118 is fluidly connected to the post-carbon filtration unit 116. The storage unit 118 is configured to receive the purified water from the post-carbon filtration unit 116 for usage. The storage unit 118 comprises a disc member 120, and a micro switch 122.

[0048]In one embodiment herein, the disc member 120 is configured to detect a flow level of the purified water in the storage unit 118, thereby transmitting a signal upon reaching a threshold value. The disc member 120 comprises a mechanical linkage to operate the inlet valve 104 without requiring an external power source.

[0049]In one embodiment herein, the micro switch 122 is connected to the disc member 120. The micro switch 122 is configured to receive the signal from the disc member 120, thereby activating the inlet valve 104 to receive the wastewater into the filtering unit 102. The micro switch 122 is configured to deactivate the inlet valve 104 to restrict the wastewater into the filtering unit 102 upon exceeding the threshold value of the purified water in the storage unit 118.

[0050]In one embodiment herein, the pump 124 is configured to generate a pressure for transferring the wastewater from the solenoid valve 108 to the first desalination unit 106. In one embodiment herein, the system 100 comprises a flow sensor 128 and a flow restricting member 130. In one embodiment herein, the flow sensor 128 is positioned between the post-carbon filtration unit and the storage unit. The flow sensor 128 is configured for measuring a flow rate to the purified water. In particular, the flow sensor 128 is configured to detect abnormal water flow rates and alert a user via a control unit. The flow sensor 128 continuously measures real-time flow rate and activates a bypass mechanism in case of extreme pressure drops.

[0051]In one embodiment herein, the flow restricting member 130 is positioned between the RO filtration unit 114 and the control valve 126. The flow restricting member 130 is configured for ensuring unidirectional flow of unpurified water while regulating pressure and preventing backflow. In one embodiment herein, the first desalination unit 106 and the second desalination unit 112 are a first antiscalant and a second antiscalant.

[0052]In one embodiment herein, the system 100 aims to minimize reject water in domestic RO systems by incorporating a dual-path antiscalant mechanism, thereby enabling partial reuse of reject water. The system 100 enhances efficiency while maintaining optimal functionality without operational or maintenance issues. The system 100 effectively reduces reject water by 50 % compared to conventional RO systems, thereby achieving an improved recovery rate of 53 % with a demonstrated lifespan of at least 7,200 liters.

[0053]According to another embodiment of the invention, FIG. 2A refers to a block diagram 200 a basic configuration. According to another embodiment of the invention, FIG. 2B refers to a block diagram 202 of an enhanced configuration with ESCS. According to another embodiment of the invention, FIG. 2C refers to a block diagram 204 of an optimized configuration with two stage antiscalant.

[0054]In one embodiment herein, the basic configuration without two stage antiscalant (SHMP -Sodium Hexametaphosphate) and Electronic Scale Control System (ESCS) is designated as Unit-1. The enhanced configuration, incorporating an ESCS unit before the RO membrane, is referred to as Unit-2. The optimized configuration, integrating two stage antiscalant with SHMP cartridges, is designated as Unit-3. In particular, Unit-3 includes one antiscalant / SHMP cartridge placed before the RO membrane and another antiscalant cartridge treating 50% of the reject water before redirecting it back to the feed supply.

[0055]In one example embodiment herein, the test water was prepared with a Total Dissolved Solids (TDS) concentration of 1500 ppm, adjusted using CaCl2, MgSO4, NaHCO3, and NaCl. The hardness, expressed as CaCO3, was maintained between 500-600 ppm, while the alkalinity, also expressed as CaCO3, ranged from 300-350 ppm. The pH levels varied between 7.2 and 7.9. All three units were tested under identical water quality conditions, using freshly prepared test water for each run. There was no recirculation of the test water. The reject flow was set at 250 ml/min for all units at the beginning of the test, and the input water pressure was maintained at approximately 1 kg/cm².

[0056]The performance analysis of Unit-1 revealed that, without any scale prevention mechanism, the membrane experienced rapid clogging. The total permeate water filtration achieved was 650 liters, beyond which the membrane was fully choked. The recovery rate started at 55% but dropped significantly to 8% by the time the unit failed. Similarly, Unit-2, which included an Electronic Scale Control System (ESCS) before the membrane, did not show a significant performance improvement over Unit-1. The total permeate filtration achieved was 650 liters, and the recovery rate ranged between 55% and 11% before the unit's output reduced to a dropwise flow, leading to test termination.

[0057]In contrast, Unit-3, which was fitted with two-stage antiscalant / SHMP cartridges and operated with a flow restrictor valve set at 250 ml/min, demonstrated substantially improved performance. The total permeate water filtration achieved was 7,200 liters, which is more than ten times the filtration capacity of Units 1 and 2. The TDS rejection rate ranged between 91.15% and 98.20%, with an average of 95.10%. The water recovery rate varied between 47.1% and 59.09%, with an average of 52.7%. The membrane remained functional without severe clogging, and testing was terminated at 7,200 liters of filtration.

[0058]Unit-4 was tested with the same two-stage antiscalant /SHMP configuration as Unit-3, but the flow restrictor valve was adjusted to 150 ml/min instead of 250 ml/min. The total permeate water filtration achieved was 3,250 liters, after which the membrane output dropped sharply to nearly zero. The TDS rejection rate ranged between 90.38% and 96.07%, averaging 91.37%. The water recovery rate varied between 47.17% and 62.07%, with an average of 58.06%. However, reducing the flow restrictor valve to 150 ml/min significantly decreased the membrane lifespan, causing early fouling and performance deterioration.

[0059]The introduction of dual-stage antiscalant /SHMP cartridges and partial reject water recirculation significantly improved system efficiency such as the membrane lifespan was extended, enabling 7,200 liters of permeate water filtration, while also facilitating surface washing of the membrane and backflushing of the copper cartridge. The average TDS rejection was recorded at 95.10%, ensuring high-quality water purification. The average water recovery rate was 52.7%, effectively minimizing water wastage. The optimal flow restrictor valve setting was identified as 250 ml/min to achieve the above benefits. A further reduction to 150 ml/min had a detrimental effect, cutting membrane life by more than 50% due to excessive pressure buildup and increased fouling.

[0060]The integrating two stage antiscalant /SHMP cartridges and optimizing flow restriction significantly enhance RO system performance. The optimized Unit-3 configuration demonstrated the best results, with higher recovery, reduced scaling, and extended membrane lifespan. Conversely, excessive flow restriction (as tested in Unit-4) resulted in premature clogging and reduced operational lifespan. This highlights the importance of maintaining an optimal balance between reject flow, membrane protection, and scaling prevention for sustained RO system efficiency.

[0061]Table 1:
Volume of water filtration (Liters) Input water TDS Unit - 1 Input water pressure Input water pH Output water pH
Output TDS ppm % TDS rejection Permeate flow ml/min Reject flow ml/min % recovery
Initial 1515 50 96.69 300 240 55.55 1 7.76 6.36
50 1507 35 97.68 280 240 53.85 1.1 7.71 5.85
100 1511 38 96.82 260 220 54.17 1 7.69 6.23
150 1509 39 97.41 250 200 55.55 1 7.70 5.91
200 1529 45 97.06 200 260 43.48 1.1 7.60 5.68
250 1513 58 96.17 180 160 52.94 1.1 7.59 5.79
300 1547 58 95.60 160 230 41.02 1.1 7.59 5.67
350 1496 51 96.59 150 220 40.54 1.1 7.60 5.37
400 1510 64 95.76 100 160 35.29 1.1 7.69 5.84
450 1512 74 95.10 100 150 38.46 1.1 7.69 6.04
500 1519 100 93.48 80 190 29.67 1.2 7.80 6.0
550 1521 124 91.45 40 90 30.76 1.1 7.71 5.91
600 1515 154 89.17 30 80 27.27 1.2 7.74 5.0
650 1486 196 83.47 10 110 8.33 7.70 6.92

[0062]The performance evaluation of Unit-1 in terms of water filtration capacity, TDS rejection efficiency, permeate flow rate, reject flow rate, recovery percentage, and pH variations highlights the gradual decline in its effectiveness over time. The initial TDS rejection rate was 96.69% at the beginning of the test, ensuring high-quality water filtration. However, as filtration progressed, the efficiency steadily declined, with the rejection rate dropping to 83.47% after 650 liters of filtration. This decline indicates increasing membrane fouling, reducing its ability to filter dissolved solids effectively.

[0063]The permeate flow rate, which started at 300 ml/min, also exhibited a continuous reduction as the system processed more water. By the time 650 liters had been filtered, the permeate flow had dropped significantly to just 10 ml/min, suggesting a progressive clogging of the membrane. This reduced water output is a clear sign of membrane fouling, likely caused by the accumulation of scale and particulate matter on the membrane surface. The reject flow rate, which started at 240 ml/min, fluctuated throughout the test, ranging from 80 ml/min to 260 ml/min at different filtration stages. The variation in reject flow suggests that the unit attempted to maintain operational balance but was unable to prevent scaling and deposition, leading to increased resistance in water flow.

[0064]The percentage of water recovery, which is a crucial indicator of system efficiency, began at a satisfactory 55.55%. However, as membrane fouling increased, the recovery percentage dropped sharply. By the time 650 liters of filtration had been completed, the recovery rate had fallen drastically to 8.33%, indicating that most of the incoming water was being wasted as reject water rather than being converted into usable filtered water.

[0065]Another key observation was the pH variation in both input and output water. The input water pH remained stable throughout the test, fluctuating slightly between 7.60 and 7.80. However, the output water pH exhibited a downward trend, reaching as low as 5.00 at 600 liters of filtration. This acidification of the output water further supports the evidence of membrane fouling and chemical reactions occurring due to scale buildup.

[0066]Ultimately, after 650 liters of filtration, Unit-1 became ineffective as the TDS rejection rate fell below 85%, the permeate flow was nearly negligible, and the water recovery percentage was extremely low. This rapid decline in performance highlights the necessity for scale prevention measures such as chemical dosing (e.g., SHMP) or electronic scale controllers (ESCs) to extend membrane life and maintain consistent filtration efficiency over an extended period.

[0067]Table 2:
Volume of water filtration (Liters) Input water TDS Unit - 2 Input water pressure Input water pH Output water pH
Output TDS ppm % TDS rejection Permeate flow ml/min Reject flow ml/min % recovery
Initial 1515 61 95.97 260 240 52 1 7.76 6.27
50 1507 46 96.95 260 230 53.06 1.1 7.71 5.48
100 1511 44 97.09 250 200 55.55 1 7.69 5.99
150 1509 62 95.89 220 130 52.86 1 7.70 5.56
200 1529 41 97.32 200 270 42.55 1.1 7.60 5.56
250 1513 49 96.76 200 220 47.62 1.1 7.59 5.59
300 1547 58 96.25 180 280 39.13 1.1 7.59 5.63
350 1496 56 96.26 170 220 43.59 1.1 7.60 5.47
400 1510 73 95.16 100 180 35.71 1.1 7.69 5.98
450 1512 82 94.58 100 180 35.71 1.1 7.69 6.09
500 1519 111 92.69 80 170 32 1.2 7.80 6.48
550 1521 148 90.27 40 160 20 1.1 7.71 6.39
600 1515 148 90.23 30 80 33.33 1.2 7.74 4.89
650 1486 184 82.19 10 80 11.11 7.70 6.95

[0068]The performance of Unit-2 in water filtration was assessed based on total dissolved solids (TDS) rejection efficiency, permeate flow rate, reject flow rate, water recovery percentage, and pH variations over time. Initially, the unit demonstrated a TDS rejection rate of 95.97%, ensuring high-quality filtration. However, as filtration progressed, the rejection efficiency gradually decreased, reaching 82.19% after filtering 650 liters of water. This decline indicates membrane fouling and a reduction in filtration effectiveness.

[0069]The permeate flow rate, which started at 260 ml/min, showed a significant decrease over time, dropping to just 10 ml/min at 650 liters of filtration. This decline is a clear sign of membrane clogging, which reduces the system’s ability to produce clean water efficiently. Simultaneously, the reject flow rate initially at 240 ml/min, fluctuated throughout the test, ranging between 80 ml/min and 280 ml/min, suggesting varying operational conditions affecting the membrane performance.

[0070]The water recovery percentage, which represents the ratio of filtered water to total input water, started at a satisfactory 52%. However, as the membrane degraded, the recovery percentage gradually declined, reaching just 11.11% at 650 liters, indicating that a large portion of the input water was being wasted. This drastic drop in recovery rate highlights significant membrane fouling and scaling, which hindered efficient water filtration.

[0071]The pH variations were also monitored throughout the process. The input water pH remained stable, fluctuating between 7.60 and 7.80. However, the output water pH exhibited fluctuations, dropping to 4.89 at 600 liters, indicating increasing acidity in the filtered water. Such a drop in pH is often associated with membrane deterioration and chemical interactions due to prolonged filtration.

[0072]Overall, Unit-2 experienced a substantial decline in performance over the course of 650 liters of filtration. The decreasing TDS rejection rate, declining permeate flow, reduced recovery percentage, and fluctuating output pH indicate severe membrane fouling and inefficiency in long-term filtration. To maintain optimal performance, the system would require periodic membrane cleaning or preventive measures, such as chemical dosing or electronic scale controllers, to minimize fouling and ensure sustained filtration efficiency.

[0073]Table 3:
Volume of
filtration Liters Unit- 3 Input water pressure Input water pH Output water pH
Input water TDS
ppm Output TDS
ppm %TDS
rejection Permeate Flow
ml/min Reject Flow
ml/min %
Recovery
Initial 1515 62 95.91 230 250 47.92 1 7.76 6.36
50 1507 46 96.95 270 240 52.94 1 7.81 5.87
100 1511 41 97.29 270 220 55.10 1 7.71 6.23
250 1530 32 97.88 280 290 49.12 1.1 7.60 5.79
1500 1511 40 98.02 280 240 53.84 1.1 7.74 5.0
1750 1500 30 97.03 250 220 53.19 1.1 7.74 5.56
2000 1515 31 97.96 250 220 52.17 1.4 7.69 5.51
4000 1588 170 89.29 200 300 40.0 1.8 7.32 6.01
4250 1615 143 91.15 210 60 ## 77.8 1.9 7.60 5.35
4500 1493 116 92.23 230 200 53.5 1.9 7.78 5.99
4750 1543 86 94.43 200 120 62.5 1.9 7.74 5.85
6750 1524 96 93.70 180 210 46.15 1.7 7.64 5.82
7000 1582 210 86.73 180 160 52.94 1.8 7.75 5.54
7200 1460 60 95.89 250 200 55.55 1.8 7.43 5.41

[0074]RO membrane was washed with water on the top and between circles with tap water, Reject water valve (adjustable) was also cleaned to remove salt deposition, SHMP pouch cleaning was given 5700Lit.

[0075]The filtration performance of Unit-3 was evaluated over 6,250 liters based on TDS rejection efficiency, permeate flow, reject flow, recovery percentage, and pH variations. Initially, the unit showed a TDS rejection rate of 95.91%, ensuring effective filtration. As filtration continued, the rejection rate fluctuated, reaching a peak of 98.20% at 1500 liters but gradually declining to 93.70% by 6,750 liters, indicating a decrease in membrane efficiency over time.

[0076]The permeate flow rate, which started at 230 ml/min, remained relatively stable in the early stages but began to decline beyond 3,750 liters, eventually dropping to 110 ml/min at 6,000 liters. This reduction suggests membrane fouling, which reduces the system’s ability to produce clean water. The reject flow rate fluctuated between 180 and 310 ml/min, indicating variations in operational efficiency and possible pressure inconsistencies.

[0077]The water recovery percentage, which measures the proportion of input water converted into usable water, remained above 50% for most of the test, peaking at 62.5% at 4,750 liters. However, recovery rates showed inconsistencies, with a significant drop to 35.48% at 6,000 liters, further indicating reduced efficiency due to membrane fouling or increased resistance in the system.

[0078]The pH variations were also monitored throughout the process. The input water pH remained stable between 7.32 and 7.98, indicating minimal fluctuation. However, the output water pH fluctuated throughout the process, reaching a low of 5.0 at 5,500 liters and a high of 6.36 initially. The pH drop towards the later stages could indicate the accumulation of acidic components or the impact of membrane degradation.

[0079]Overall, Unit-3 demonstrated strong filtration performance initially, but efficiency declined after prolonged use. The drop in TDS rejection, decreasing permeate flow, and fluctuating recovery rates suggest membrane fouling and potential clogging issues over time. To maintain optimal performance, periodic membrane cleaning or preventive maintenance would be necessary to sustain high water quality and maximize recovery efficiency. The variance in the output pH can be adjusted by incorporating the pH balancing mineral addition in the post carbon cartridge.

[0080]Table 4:
Volume of
filtration Liters Unit- 4 Input water pressure Input water pH Output water pH
Input water TDS
ppm Output TDS
ppm %TDS
rejection Permeate Flow
ml/min Reject Flow
ml/min %
Recovery
Initial 1477 58 96.07 250 180 58.14 1.9 7.54 6.26
50 1588 128 91.94 180 120 60.00 1.5 7.32 6.01
100 1486 114 92.33 160 120 57.14 1.8 7.69 5.83
250 1588 107 93.26 260 200 56.52 1.8 7.74 6.04
500 1586 104 93.44 250 150 62.50 1.9 7.76 5.88
750 1539 194 87.39 260 110 70.27 1.9 7.49 5.64
1000 1571 126 91.98 270 180 60.00 1.9 7.92 5.0
1250 1574 116 92.63 250 280 47.17 1.9 7.86 5.58
1500 1575 108 93.14 240 240 50.00 1.8 7.43 5.26
1750 1670 98 94.13 220 180 55.00 1.1 7.94 5.88
2000 1556 139 91.07 230 160 58.97 1.2 7.95 6.43
2250 1438 109 92.42 220 140 61.11 1.3 7.61 5.28
2500 1580 152 90.38 200 140 58.82 1.4 7.77 5.16
2750 1584 95 94.00 220 150 59.46 1.4 7.41 6.38
3000 1710 157 90.82 180 110 62.07 1.5 7.62 6.17
3250 1491 343 77.00 140 130 51.85 1.8 7.23 5.84
3300 xx xx xx dropwise 130 xx 1.8 7.41 5.96

[0081]The filtration performance of Unit-4 was evaluated over 3,300 liters, focusing on TDS rejection, permeate flow, reject flow, recovery percentage, and pH stability. Initially, the system showed a TDS rejection rate of 96.07%, which decreased over time, dropping significantly to 77.00% at 3,250 liters, indicating a decline in membrane efficiency. The highest rejection rate observed was 94.13% at 1,750 liters, suggesting fluctuations in performance.

[0082]The permeate flow rate started at 250 ml/min, remained stable at 1.8–1.9 ml/min for most of the process, but sharply declined beyond 3,250 liters, where water was coming out only dropwise. This drastic reduction indicates severe membrane fouling or clogging issues, significantly affecting filtration efficiency. The reject flow rate, which varied between 110 ml/min and 280 ml/min, also showed inconsistencies, suggesting potential operational inefficiencies or variations in input conditions.

[0083]The water recovery percentage remained above 50% in most cases, peaking at 70.27% at 750 liters, which indicates effective filtration at this stage. However, recovery rates fluctuated, with a notable decline towards 3,250 liters, reflecting membrane degradation and reduced efficiency.

[0084]The pH levels were relatively stable throughout the filtration process. The input water pH ranged between 7.23 and 7.95, while the output water pH varied between 5.0 and 6.43, indicating a slight acidification of the permeate water, particularly at 1,000 liters and beyond. This suggests potential accumulation of acidic compounds or membrane material degradation affecting water chemistry.

[0085]Overall, Unit-4 demonstrated effective filtration in the early stages, with a high TDS rejection rate, good permeate flow, and stable recovery efficiency. However, efficiency declined beyond 3,000 liters, with a significant drop in TDS rejection, reduced permeate flow to a dropwise rate, and fluctuating recovery percentage. The observed decline suggests that membrane fouling, clogging, or pressure inconsistencies have impacted the filtration process, requiring maintenance or membrane replacement to restore optimal performance.

[0086]According to another embodiment of the invention, FIG. 3 refers to a block diagram of a reverse osmosis (RO) water filtration system 300. In one embodiment herein, the feed water enters into the system 100 via the inlet valve 104 and directed into the filtering unit 102, which is the initial stage to remove large particles such as dirt and rust, thereby preventing damage to subsequent filters.

[0087]Next, the feed water flows through the solenoid valve 108 that is electronically controlled component for regulating the flow of the feed water. Next, the pump 124 boosts the feed water with the pressure to the pre-carbon filtration unit 110. Later, the pre-carbon filtration unit 110 absorbs chlorine and organic contaminants from the feed water and transfers the feed water to the RO filtration unit 114. Next, the RO filtration unit 114 removes dissolved solids, heavy metals, bacteria, and other impurities from the feed water, thereby ensuring high-purity water output i.e., the purified water.

[0088]The flow restricting member 130 regulates the rejected water flow and assists in maintaining the required pressure inside the RO filtration unit 114, thereby preventing excessive water loss. The purified water moves through the post-carbon filtration unit 116 for enhancing the taste and removing any remaining odors or chemicals. Finally, the purified water is stored in the storage unit 118. The disc member 120 and the micro switch 122 monitor the level of the storage unit 118 and shut off the inlet valve 104 when the storage unit 118 is full to prevent overflow.

[0089]According to another embodiment of the invention, FIG. 4 refers to a block diagram of a high-recovery reverse osmosis (RO) water filtration system 400 incorporating an Energy Saving Controller (ESC). In one embodiment herein, initially, the feed water is entered into the filtering unit 102 via the inlet valve 104 and removes the large particles, such as sand, rust, and dirt, ensuring that the water entering the subsequent filtration stages is free of these contaminants. The solenoid valve 108, which is an electronically controlled component, regulates the flow of the feed water into the system 100, ensuring a consistent water supply.

[0090]The pump 124 is responsible for increasing the pressure of the feed water, thereby ensuring that the feed water is effectively pushed through the pre-carbon filtration unit 110. The pre-carbon filtration unit 110 removes the chlorine, organic compounds and odors from the feed water. The RO filtration unit 114 removes the dissolved salts, heavy metals, bacteria, viruses, and other impurities. The flow restricting member 130 controls the flow of reject water, maintaining the appropriate pressure within the RO filtration unit 114.

[0091]Once the feed water passes through the RO filtration unit 114, the system 400 uses the control valve 126 to regulate the outflow of the reject water, which contains the impurities removed during filtration. The next stage is the post-carbon filtration unit 116, which acts as the final filtration step, polishing the water and removing any remaining odors and chemicals, improving its taste.

[0092]The purified water is then stored in the storage unit 118 for future use. The disc member 120 and the micro switch 122 are vital components that monitor the purified water level inside the storage tank. The disc member 120 detects the water level, and when the storage unit 118 is full, the micro switch 122 shuts off the inlet valve 104 to prevent overflow. Additionally, the flow sensor 128 tracks the water flow rate, helping to control the operation of the system 400. The system 400 also includes an NRV (Non-Return Valve), which ensures that water flows in one direction, preventing any backflow.

[0093]The ESC 132 helps in managing the various components of the system 400 by providing real-time monitoring and control over water flow rates, pressure levels, and filtration status. It interfaces with the solenoid valve 108, the Pump 124, and the flow sensor 128, thereby allowing for automatic adjustments based on system performance. The ESC 132 optimizes the efficiency of the RO filtration unit 114 and ensures that the entire filtration process is running smoothly, preventing system overloads or inefficiencies.

[0094]The high-recovery reverse osmosis (RO) water filtration system 400 incorporating with ESC technology, operates effectively to remove a wide range of impurities from water, making it safe and clean for consumption. With its multiple filtration stages, automated controls, and monitoring components, including real-time adjustments and enhanced efficiency, the system ensures both reliability and optimal performance in providing purified water.

[0095]According to another embodiment of the invention, FIG.5 refers to a flowchart 500 of a method for operating the system 100 for descaling reverse osmosis membranes. At step 502, the filtering unit 102 receives the feed water through the inlet valve 104 and removes sediments from the feed water. At step 504, the first antiscalant unit 106 receives the feed water from the filtering unit 102 and partial recycled reject water and prevents a scale formation caused by dissolved salts, minerals and hardness in the feed water.

[0096]At step 506, the pre-carbon filtration unit 110 receives the feed water and partial recycled reject water from the first antiscalant unit 106 and removing one or more chemical contaminants in the feed water. At step 508, the second antiscalant unit 112 receives the feed water from the pre-carbon filtration unit 110 and prevents the scale formation due to excess minerals and hardness in the feed water and the partial recycled reject water.

[0097]At step 510, the RO filtration unit 114 receives the feed water and the partial recycled reject water from the second antiscalant unit 112 and removes the minerals, heavy metals, microorganisms and other impurities in the feed water and the partial recycled reject water, thereby separating purified water and the un-purified water from the feed water and the partial recycled reject water. At step 512, the post-carbon filtration unit 116 receives the purified water from the RO filtration unit 114 and removes residual chlorine, odors or tastes in the purified water so as to improve water quality. At step 514, the storage unit 118 receives the purified water from the post-carbon filtration unit 116 for usage.

[0098]Numerous advantages of the present disclosure may be apparent from the discussion above. In accordance with the present disclosure, a system and method for descaling reverse osmosis membranes using electrochemically / two stage antiscalant treated reject water. The proposed system 100 increases the recovery rate of RO systems is increased to at least 53 %.

[0099]The proposed system 100 reduces water wastage from the RO purifiers by at least 50%, thereby minimizing environmental impact and conserving precious water resources. The proposed system develops an efficient and cost-effective method for descaling RO membranes using an electrochemical / two stage antiscalant processes, thereby reducing reliance on promoting responsible water management. The proposed system 100 is easily installable and adaptable to existing RO purifiers so as to make accessible to a broader user base.

[0100] The proposed system 100 is cost-effective and energy-efficient solution that can be implemented widely for domestic water purification, offering economic and environmental benefits. The proposed system 100 utilizes the rejected high-TDS water from RO systems for further purification and reuse for non-potable purposes, maximizing water utilization and reducing drain water. The proposed system 100 prolongs the lifespan of preventing scaling and fouling through electro-descaling or SHMP-based scale inhibition, minimizing maintenance and replacement costs.

[0101]It will readily be apparent that numerous modifications and alterations can be made to the processes described in the foregoing examples without departing from the principles underlying the invention, and all such modifications and alterations are intended to be embraced by this application.
,CLAIMS:5. CLAIMS:
I / We Claim:
1.A system (100) for descaling reverse osmosis membranes, comprising:
a filtering unit (102) configured to receive wastewater through an inlet valve (104) and remove sediments from the wastewater;
a first antiscalant unit (106) fluidly connected to the filtering unit (102) via a solenoid valve (108) and a pump (124), wherein the first antiscalant unit (106) is configured to receive the recycled reject water from the filtering unit (102) and prevent a scale formation caused by dissolved salts, minerals, and hardness in the wastewater;
a pre-carbon filtration unit (110) fluidly connected to the first desalination unit (106), wherein the pre-carbon filtration unit (110) is configured to receive the wastewater from the first antiscalant unit (106) and remove one or more chemical contaminants in the wastewater;
a second antiscalant unit (112) fluidly connected to the pre-carbon filtration unit (110), wherein the second antiscalant unit (112) is configured to receive the combined feed water from the pre-carbon filtration unit (110) and minimize or prevent the scale formation due to dissolved salts and hardness minerals in the wastewater;
a reverse osmosis (RO) filtration unit (114) fluidly connected to the second antiscalant unit (112), wherein the RO filtration unit (114) is configured to receive the wastewater from the second antiscalant unit (112) and minimizes or reduces the scale formation due to excess minerals, salts, microorganisms and impurities in the wastewater, thereby separating purified water and un-purified water from the wastewater;
a post-carbon filtration unit (116) fluidly connected to the RO filtration unit (114), wherein the post-carbon filtration unit (116) is configured to receive the purified water from the RO filtration unit (114) and remove residual chlorine, odors or tastes in the purified water so as to improve water quality; and
a storage unit (118) fluidly connected to the post-carbon filtration unit (116), wherein the storage unit (118) is configured to receive the purified water from the post-carbon filtration unit (116) for usage.
2.The system (100) as claimed in claim 1, wherein the storage unit (118) comprises:
a disc member (120) configured to detect a flow level of the purified water in the storage unit (118), thereby transmitting a signal upon reaching a threshold value; and
a micro switch (122) connected to the disc member (120), wherein the micro switch (122) is configured to receive the signal from the disc member (120), thereby activating the inlet valve (104) to receive the wastewater into the filtering unit (102),
wherein the micro switch (122) is configured to deactivate the inlet valve (104) to restrict the wastewater into the filtering unit (102) upon exceeding the threshold value of the purified water in the storage unit (118).
3.The system (100) as claimed in claim 1, wherein the one or more chemical contaminants include at least one of chlorine and organic impurities.
4.The system (100) as claimed in claim 1, wherein the pump (124) is configured to generate a pressure for transferring the wastewater from the solenoid valve (108) to the first antiscalant unit (106).
5.The system (100) as claimed in claim 1, wherein the un-purified water is transferred out from the RO filtration unit (114) through a control valve (126).
6.The system (100) as claimed in claim 1, wherein the first antiscalant unit (106) minimizes the scale formation due to excess dissolved salts and minerals from the reject water via the control valve (126), thereby ensuring efficient separation and transfer of impurities.
7.The system (100) as claimed in claim 1, wherein the system (100) comprises:
a flow sensor (128) positioned between the post-carbon filtration unit (116) and the storage unit (118),
wherein the flow sensor (128) is configured for measuring a flow rate to the purified water.
8.The system (100) as claimed in claim 1, wherein the system (100) comprises
a flow restricting member (130) positioned between the RO filtration unit (114) and the control valve (126),
wherein the flow restricting member (130) is configured for ensuring unidirectional flow of unpurified water while regulating pressure and preventing backflow.
9.The system (100) as claimed in claim 1, wherein the first antiscalant unit (106) and the second antiscalant unit (112) are a first SHMP and a second SHMP.
10.A method for operating a system (100) for descaling reverse osmosis membranes, comprising:
receiving, by a filtering unit (102), feed water through an inlet valve (104) and removing sediments from the feed water;
receiving, by first antiscalant unit (106), the feed water from the filtering unit (102) and partial recycled reject water and preventing a scale formation caused by dissolved salts, minerals and hardness in the feed water;
receiving, by a pre-carbon filtration unit (110), the feed water and partial recycled reject water from the first antiscalant unit (106) and removing one or more chemical contaminants in the feed water;
receiving, by a second antiscalant unit (112), the feed water from the pre-carbon filtration unit (110) and preventing the scale formation due to excess minerals and hardness in the feed water and the partial recycled reject water;
receiving, by a reverse osmosis (RO) filtration unit (114), the feed water and the partial recycled reject water from the second antiscalant unit (112) and removing the minerals, heavy metals, microorganisms and other impurities in the feed water and the partial recycled reject water, thereby separating purified water and the un-purified water from the feed water and the partial recycled reject water;
receiving, by a post-carbon filtration unit (116), the purified water from the RO filtration unit (114) and removing residual chlorine, odor or tastes in the purified water so as to improve the water quality; and
receiving, by a storage unit (118), the purified water from the post-carbon filtration unit (116) for usage.