Title of Invention	A PROCESS FOR IMPROVING FLUX OF LIQUID
Abstract	A process for improving flux of a liquid in separation technique by using membranes, the process comprising passing a liquid from a outlet (2) of a liquid supply (1) at the controlled rate through a fluid communication (3) and a inlet (4) to a activated carbon unit (5) to filter the liquid and remove odoriferous material; passing the filtered liquid from a outlet (6) of the activated carbon unit (5) under controlled pressure using pump through a fluid communication (7) and an inlet (8) to a membrane unit (9) to obtain pure liquid and reject the brine liquid; passing the pure liquid from a outlet (10) of the membrane unit through a fluid communication (11) and an inlet (12) to a reservoir (12) characterized in that the outlet (10) of the membrane unit (9) being vacuumised in the range of 10 to 700 mm Hg by applying vacuum pump (14) at the outlet (10) or by increasing vertical distance between outlet (10) of the membrane unit (9) and reservior (13) depending on the feed temperature of the liquid which being below the boiling point of the liquid, to increasing flux of liquid is disclosed. A device for improving the flux of the liquid is also disclosed. Its use in water purification and increasing concentration of sugars in sugar cane juice in sugar industry is also disclosed.

Title of Invention

A PROCESS FOR IMPROVING FLUX OF LIQUID

Abstract

A process for improving flux of a liquid in separation technique by using membranes, the process comprising passing a liquid from a outlet (2) of a liquid supply (1) at the controlled rate through a fluid communication (3) and a inlet (4) to a activated carbon unit (5) to filter the liquid and remove odoriferous material; passing the filtered liquid from a outlet (6) of the activated carbon unit (5) under controlled pressure using pump through a fluid communication (7) and an inlet (8) to a membrane unit (9) to obtain pure liquid and reject the brine liquid; passing the pure liquid from a outlet (10) of the membrane unit through a fluid communication (11) and an inlet (12) to a reservoir (12) characterized in that the outlet (10) of the membrane unit (9) being vacuumised in the range of 10 to 700 mm Hg by applying vacuum pump (14) at the outlet (10) or by increasing vertical distance between outlet (10) of the membrane unit (9) and reservior (13) depending on the feed temperature of the liquid which being below the boiling point of the liquid, to increasing flux of liquid is disclosed. A device for improving the flux of the liquid is also disclosed. Its use in water purification and increasing concentration of sugars in sugar cane juice in sugar industry is also disclosed.

Full Text	FORM 2 THE PATENT ACT 1970 (39 of 1970) & The Patents Rules, 2003 COMPLETE SPECIFICATION (See section 10 and rule 13) 1. TITLE OF THE INVENTION: A process for improving flux of liquid 2 APPLICANT (a) Name : Malshe Vinod Chintamani (b) Nationality : Indian (c) Address : 1, Staff Quarters, UDCT Campus, Matunga, Mumbai - 400 019, Maharashtra, India 3. INVENTORS (a) Name : Malshe, Vinod Chintamani (b) Nationality Indian (c) Address 1, Staff Quarters, UDCT Campus, Matunga, Mumbai - 400 019. Maharashtra, India (a) Name Damle, Aditi Sharad (b)Nationality : Indian (c) Address : 1, Staff Quarters, UDCT Campus, Matunga, Mumbai - 400 019. Maharashtra, India 3. PREAMBLE TO THE DESCRIPTION The following specification particularly describes the invention and the manner in which it is to be performed. Technical Field: The present invention relates to a process for improving flux of liquid in separation technique using membranes. The present invention also relates to a device, which improves the flux of a liquid in separation technique using membranes. The present invention relates to improving the flux of a liquid without sacrificing separation of ultrafiltration, nanofiltration and reverse osmosis devices by activating the finer pores for home or industrial, municipal use like water purification system and sugar purification, etc. The present invention relates to use of the above process and device in water purification, sugar purification and the like end application. Background and Prior Art: Water is the most required commodity for homes and industry. More than 98% of the water available on earth is seawater, which is unfit for human consumption. Most of the fresh water on the surface of earth is either having high total dissolved solids (TDS) or bacterial contamination and needs to be purified. Of the various methods such as multiple effect evaporation, ion exchange and reverse osmosis available, the last method is the most preferred because it saves chemicals and energy. The water concentrated with minerals formed in the reverse osmosis can be simply discharged to the starting body of water. In the modern medically and scientifically advanced world, people are more conscious about their health and improve and maintain the quality of drinking water by removing undesired salts and minerals. In household as well as commercial reverse osmosis (RO) plant; an active carbon (charcoal) unit is utilized as filter and an adsorbant to remove elemental chlorine and organic impurities. Charcoal removes odoriferous and colouring materials contained in water. Reverse osmosis, a purification technique based on membrane technology, became commercially viable in the 1970's and has become central technology in high purity water processing. Today, state of the art industrial or household high purity water systems utilize some or all the technologies like pretreatment, sand filtration, carbon treatment, softening, reverse osmosis, deionization, UV treatment, filtration in combination to provide water that approaches the theoretical ideal for pure water. 2 Stage I: Fine filtration to remove the suspended solids to a very low level defined by silt density index. This operation is carried out by either sand filters or cartridge filters involving various materials for preparation of cartridges. This includes fibres of polypropylene, polyester, glass or stainless steel. Disinfection of the water is carried out with ozonation, chlorination, bromination, ultraviolet light and the residual oxidizing agent such as chlorine and organics are removed with activated Carbon, which also removes organic matter and chemical smell. Stage II: Cellulose acetate or TFC (Thin Film Composite) Polyamide Membrane is used to remove the dissolved salts. The membranes also remove organic matters, germs, bacteria, virus, compound metals and harmful chemicals such as residues of pesticides. The pure water is collected at the end of stage II at atmospheric pressure. In the separation of water, if the layer of pure water is removed by the application of pressure, the salts gets concentrated on the surface and have to move away to the bulk by the process of diffusion. This effectively increases osmotic pressure of the solution very close to membrane surface. Thus the external pressure is substantially neutralized by osmotic pressure of concentrated salts present next to pure water layer and available force for pushing water across the pore is represented by "Applied pressure-Osmotic pressure at the interface". Therefore from the principle of hydrostatics, if one compares flow rate of salt solution across a membrane with the same flow rate of pure water (Pure Water 3 Permeability or PWP) across the membrane, the difference in applied pressure in the two cases would represent osmotic pressure of that solution on the interface. Thus the net driving force in a RO process is the difference of pressure between the applied pressure and the osmotic pressure at the interface. Higher the salt content of the water, more is the osmotic pressure at the interface for a given flux and thus lower is the flux. If one attempts to draw more product by applying higher pressure, more water does get out of the membrane but due to proportional rise in the osmotic pressure the net effect is very low. A membrane has pores of various dimensions on the surface. The separation takes place by adsorption of pure water on the surface and the dissolved salts are repelled or negatively adsorbed on the interface. Thus more are the dissolved solid, higher is the osmotic pressure at the interface and thus lower is the flux. Thus in a RO process, the recovery of water is a direct function of the dissolved salts. Higher the dissolved salts, lower is the recovery. Thus in a typical sea water membrane operation, the water is required to be pushed at a very high pressure of about 70 kg/ cm .Of this water only a small portion, less than 30%, can be recovered and the balance has to be discarded. Thus, the effort made in pretreating the large quantity of water is wasted. Efforts to improve the recovery of the water beyond this require modifying the entire membrane product to suit high pressure requirement thus increasing the hardware cost disproportionately and also increasing the requirement of the pumping energy to the membrane. Objects An object of the invention is to provide a process for achieving high flux of a liquid without significant difference in separation by activating even the smallest of the pores that are not active due to the low pressure, available at the interface. Another object of the invention is to provide a process for improving flux of a liquid in the separation technique using a membrane. Another object of the invention is to provide a process, which provides a vacuum on the product side of the membrane; thus pure water layer is collected with much ease (ie. Flux is increased without any decrease in salt rejection property). Yet another object of the invention is to provide a device for improving the flux of a liquid in the separation technique using a membrane. Yet another object of the invention is to provide a device, which provides a vacuum on the product side of the membrane; thus pure water layer is collected with much ease (ie. Flux is increased without any decrease in salt rejection property). Yet another object the invention is to provide a use of the above process and device for water purification. 4 Yet another object of the invention is to provide a use of the above process and device for sugar purification. Yet another object of the invention is to provide a water purification process with the improved flux of water without affecting a salt rejection. Yet another object of the present invention is to provide a water purification device for improving the flux of water without affecting the salt rejection. Detailed Description: According to the present invention there is provided a process for improving flux of a liquid in a separation technique by using membranes, the process comprising vacuumising a outlet (10) of a membrane unit (9) on a product side in the range of 10 mm to 700 mm Hg by applying a vacuum pump (14) at the outlet (10) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and a reservoir (13) depending on a feed temperature of a liquid which is being below the boiling point of the liquid being separated. According to the present invention there is provided a process for improving flux of a liquid in separation technique by using membranes, the process comprising passing a liquid from a outlet (2) of a liquid supply (1) at the controlled rate through a fluid communication (3) and a inlet (4) to a activated carbon unit (5) to filter the liquid and remove odoriferous material; passing the separated liquid from a outlet (6) of the activated carbon unit (5) under controlled pressure using pump through a fluid communication (7) and a inlet (8) to a membrane unit (9) to obtain pure liquid and reject the brine liquid; passing the pure liquid from a outlet (10) of the membrane unit through a fluid communication (11) and a inlet (12) to a reservoir (13) characterized in that the outlet (10) of the membrane unit (9) being vacuumised in the range of 10 to 700 mm Hg by applying a vacuum pump (14) at the outlet (10) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) depending on a feed temperature of the liquid which is being below the boiling point of the liquid, to increase the flux of the liquid. According to the present invention there is provided a device for improving a flux of a liquid, the device comprising a liquid supply (1), an activated carbon (charcoal) unit (5), a membrane unit (9) and a reservoir (13); each unit including reservoir is provided with inlets and outlets; a inlet (4) of the activated carbon unit (5) being in a fluid communication (3) with a outlet (2) of the liquid supply (1), a inlet (8) of the membrane unit (9) is in a fluid communication (7) with a outlet (6) of the activated carbon unit (5), a 5 inlet (12) of the reservoir (13) being in a fluid communication (11) with a outlet (10) of the membrane unit (9) characterized in that the outlet (10) of the membrane unit (9) being vacuumised on product side in the range of 10 mm to 700 mm Hg by applying a vacuum pump (14) at the outlet (10) of the membrane unit (9) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) depending upon the feed temperature of the liquid, which is being below the boiling point of the liquid, to achieve high flux of the liquid. Preferably the membrane used in the membrane unit (9) is selected from ultrafiltration membrane, nanofiltration membrane or reverse osmosis membrane. More preferably the membranes used are cellulose acetate or composite polyamide or polysulfone or any composite membrane of suitable size and shape and has flux rate 10 m3 after applying 10 kg/cm 2 pressure. Preferably the vacuum at the outlet (10) of the membrane unit (9) is in the range of 50-400 mm Hg. Preferably the vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) is in the range of 0.01 meters to 9 meters of water column. The flux of the liquid is improved in the range of 20 % to 90 %. Preferably the feed temperature of the liquid is in the range of 2 - 40°C. Higher vacuum is applied at the lower feed water temperature. The vacuum can be applied with the help of a vacuum pump or by increasing a vertical distance between the outlet of the membrane unit and the storage tank or reservoir using barometric leg. Second alternative has an advantage of inbuilt facility for creating vacuum without mechanical work. The preferred vacuum at the outlet (10) of the membrane unit (9) is 400 mm Hg or the preferred distance between the outlet (10) of the membrane unit (9) and the reservoir (13) is 4 meter. It is easily possible to raise the entire apparatus to a higher elevation in an existing installation and it is possible to provide the facility for a new installation. The improvement in flux is more in the case of higher salt concentration compared to lower ones particularly at higher applied pressure. According to the present invention there is provided use of the process and the device to purify the water and to increase concentration of sugars in sugar cane juice in sugar industry by application of vacuum on the permeate side. According to the present invention there is provided a use of the above device to purify water, the device comprising a water supply (1), an activated carbon (charcoal) unit (5), a membrane unit (9) and a reservoir (13); each unit including the reservoir is provided with inlets and outlets; a inlet (4) of the activated carbon unit (5) being in a fluid communication (3) with a outlet (2) of the liquid supply (1), a inlet (8) of the membrane unit (9) is in a fluid communication (7) with a outlet (6) of the activated carbon unit (5), a 6 inlet (12) of the reservoir (13) being in a fluid communication (11) with a outlet (10) of the membrane unit (9) characterized in that the outlet (10) of the membrane unit (9) being vacuumised on product side in the range of 10 mm to 700 mm Hg by applying a vacuum pump (14) at the outlet (10) of the membrane unit (9) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) depending upon a feed temperature of water, which is being below the boiling point of the liquid, to achieve high flux of the water. According to the present invention there is provided a use of the above process to purify the water, the process comprising passing a water from a outlet (2) of a water supply (1) at the controlled rate through a fluid communication (3) and a inlet (4) to a activated carbon unit (5) to filter the water and remove odoriferous material; passing the filtered water from a outlet (6) of the activated carbon unit (5) under controlled pressure using pump through a fluid communication (7) and a inlet (8) to a membrane unit (9) to obtain pure water and reject the brine water; passing the pure water from a outlet (10) of the membrane unit through a fluid communication (11) and a inlet (12) to a reservoir (12) characterized in that the outlet (10) of the membrane unit (9) being vacuumised in the range of 10 to 700 mm Hg by applying a vacuum pump (14) at the outlet (10) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) depending on a feed temperature of the water which being below the boiling point of the liquid, to increase flux of liquid without affecting the salt rejection. Preferably the membrane used in the membrane unit (9) is selected from ultrafiltration membrane, nanofiltration membrane or reverse osmosis membrane. More preferably the membranes used are cellulose acetate or composite polyamide or polysulfone or any composite membrane of suitable size and shape and has flux rate 10 m3 after applying 10 kg/cm pressure. Preferably the vacuum at the outlet (10) of the membrane unit (9) is in the range of 50-400 mm Hg. Preferably the vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) is in range of 0.01 meters to 9 meters of water column. The flux of the liquid is improved in the range of 20 % to 90 % without affecting the salt rejection. Preferably the feed temperature of the water is in the range of 0 - 40°C The fluid communication means being plastic / metal pipes. The units and reservoir also are fabricated from suitable safe plastics / metals. The membrane unit is also provided with an outlet for removing urine liquid/ mineral concentrated liquid / brine liquid. The brine liquid / urine liquid is intended to apply to the liquid containing a higher concentration of undesirable ions / salts. The invention is described with the drawing and description, which follows. Figure 2 is a schematic representation of the system. 7 Referring now to the accompanying drawing: a outlet (2) of a liquid supply (1) is connected by a fluid communication (3) to a inlet (4) of an activated carbon unit (5). The liquid is supplied to the activated carbon unit (5) under controlled rate by using valve. A outlet (6) of the activated carbon unit (5) is connected by a fluid communication (7) to a inlet (8) of a membrane unit (9). The liquid filtered through the activated carbon unit (5) is supplied under pressure to the membrane unit (9) by using a pump. The cellulose fiber filter may be held in fluid communication (7) to prevent any active carbon particle from entering the membrane unit (9). The membrane unit (9) contains ultrafiltration membrane/ nanofiltration membrane / reverse osmosis membrane, either prepared from cellulose acetate or from thin composite polysulfone or polyamide or composite membrane of suitable size and shape has flux rate 10 m3 after applying 10 kg/cm 2 pressure. A outlet (10) of the membrane unit (9) is connected by a fluid communication (11) to a inlet (12) of a reservoir (13). The membrane unit is vacuumised at the other end of the membrane towards the outlet (10) by applying a vacuum pump (14) at the outlet (10) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13). The pressure created by vacuum directly regulates the flux of the liquid and salt rejection. The pure liquid is passed through the outlet (10) into the reservoir (13). The brine liquid rejected is passed through outlet (15) of the membrane unit (10) to discharge. The reservoir (13) may have an outlet means with a suitable opening valve. The brine to permeate ratio is 10-15%. Separation starts as soon as the membrane is brought in contact with the liquid, as flux and separation are the function of the total pore area and pore size distribution. If the layer of pure water is removed by application of pressure, the salts get concentrated on the surface and have to move away to the bulk by the process of diffusion. This effectively increases osmotic pressure of the solution very close to membrane surface. Thus the external pressure is substantially neutralized by osmotic pressure of concentrated salt present next to pure water layer and available force for pushing water across the pore is represented by "Applied pressure-Osmotic pressure at the interface". In the present invention we applied pressure on both the side of the membrane to overcome the osmotic pressure and thereby achieved high rate flow of water. The present method and device for water purification give much higher flux for the same applied pressure without significant difference in separation. Applied total pressure is very critical in the invention. High vacuum leads to boiling of water and disturbs the membrane operation. The separation by using the membranes is a tangential flow process where the feed stream splits into treated water (called permeate or product water) and wastewater (called reject or concentrate water) as it is processed. Contaminants present in the feed stream are 8 removed from water that passes through the membrane and concentrate in the water that remains behind. It is important to maintain adequate flow in the "concentrate" stream to prevent contaminants from depositing on the membranes. As the liquid temperature is reduced, the amount of product liquid produced is also reduced due to increase in liquid viscosity and the shrinkage of pores associated with temperature changes. The membranes may require periodic cleaning and should be cleaned if the product liquid flow-rate falls to less than 50% below normal (with feed liquid composition, temperature and pressure conditions being the same). The liquid is fed with scale control polymers or additives, acid to lower the pH to prevent crystallization of carbonates, sulfates and phosphates of calcium, magnesium and strontium. The device may be furnished with various instruments and controls to permit monitoring of its operation and performance. Pressure gauges may be provided to permit monitoring of the membrane feed and concentrate pressures. Flow meters may be provided for monitoring the product and reject stream flow rates. Conductivity monitor may be provided to measure the percent of ionized solids removed by the system (called percent rejection). The membrane unit may employ a pressure relief valve to prevent the unintentional back over pressurization of the membranes, which could damage the membranes. The system ranges from small stills, through to wall mounted water systems to industrial manufacturing water systems housed in their own buildings to vast desalinization plants occupying acres, providing drinking water from hard water. Thus by using this technique, the flux of the liquid improves to 20 to 90 % without change in the separation. This is envisaged by applying vacuum at the other surface of the membrane, which essentially provides a higher driving force for the pure water that has already been separated by adsorption of pure water by the membrane surface. Thus the net difference in the pressure across the membrane is much more than just an additional pressure equal to the vacuum applied on the front side of the membrane. The invention is further illustrated by the following examples, which should not construe the effective scope of the claims. The examples are given only to illustrate the phenomenon and are not limited to any one application. Example 1: Water in the form of saturated sodium chloride solution (1000 ppm) from water supply (1) was passed at the controlled rate ie at 5.27 kg/sq.cm using valve to an activated carbon unit (5) to filter the water and removed odoriferous material. The separated water was passed under controlled pressure of 6.12 kg/sq.cm, 8.16 kg/sq.cm and 10.20 kg/sq.cm 9 respectively using a pump to a reverse osmosis unit (9) to obtain pure water and the brine water was rejected. The reverse osmosis unit comprises commercially available composite polyamide membrane (made by Ion-Exchange Ltd). The flow rate of water into the membrane unit was 30 to 100 times more than rate of product water (i.e. cross flow). The pressure applied at the outlet (10) of the reveres osmosis unit (9) by vacuum pump is 50, 100, 150, 200, 300 and 400 mm respectively. The same experiment is repeated without applying pressure at the outlet (10) of the reverse osmosis unit (9) ie. at atmospheric pressure. The observed marked increase in flux of the water without affecting separation is shown in table 1. Table 1: Increase in flux for 1000 ppm NaCl solution Pressure Pressure applied at the inlet of the membrane unit (9) applied at the outlet (10) mm of Hg 6.12 Kg/sq.cm 8.16 Kg/sq.cm 10.20 Kg/sq.cm Flux In lmd %Increasein flux %Saltrejection Flux In lmd %Increasein flux %Saltrejection Flux In lmd /oIncrease in flux %Saltrejection Without vacuum 193.49 ™ 87.02 268.23 ™ 94.91 369.55 " 96.44 50 mm Hg 353.77 82.84 91.86 361.25 34.68 94.15 481.66 30.34 96.18 100 mm Hg 306.43 58.37 90.33 377.02 40.56 93.90 494.12 33.71 96.18 150 mm Hg 248.30 28.33 93.64 383.66 43.03 95.42 514.88 39.33 96.69 200 mm Hg 235.02 21.46 93.13 332.18 23.84 95.68 528.17 42.92 96.44 300 mm Hg 238.34 23.18 95.42 330.52 23.22 93.64 519.86 40.67 96.44 400 mm Hg 233.36 20.61 93.64 332.18 23.84 95.93 514.88 39.33 96.69 10 The table 1 indicates the flux of the water was improved without affecting the salt rejection. The flux of the water was increased with the increase in the pressure applied at the outlet (10) of the reverse osmosis unit (9). Example 2 Pure water permeability of the commercially available composite polyamide membrane (made by Ion Exchange ltd) was detected by applying pressure at the outlet (10) of the reverse osmosis membrane unit (9). The flux of the pure water should always be higher than the flux of the salt solution at any pressure that acts as a positive control for the method. Pure water was passed under controlled pressure of 5.27 kg/sq.cm using pump to a reverse osmosis unit (9). The reverse osmosis unit comprises commercially available composite polyamide membrane (made by Ion exchange ltd). The pressure applied at the outlet (10) of the reveres osmosis unit (9) by vacuum pump was 50, 100, 150, 200, 300 and 400 mm respectively. The same experiment was repeated without applying the pressure at the outlet (10) of the reverse osmosis unit (9). The observed marked increase in flux of the pure water is shown in table 2. Table 2: Pure Water Permeability Applied pressure on the membrane = 5.27 kg/sq.cm Pressure Flux in % Increase in applied at the lit/day Flux Outlet In mm of Hg 0 236.2 — 50 253.4 7.28 100 265.0 12.19 150 276.5 17.06 200 299.5 26.80 300 316.8 34.12 400 351.4 48.77 Above results of table 2 show the flux was increased with increase in applied pressure at the outlet (10). It reaches a maximum of 48.77% over initial value at atmospheric pressure (no vacuum). Example 3: Water in the form of saturated sodium chloride solution (200 ppm) from water supply (1) was passed at the controlled rate ie at 5.27 kg/sq.cm using valve to an activated carbon 11 unit (5) to filter the water and removed odoriferous material. The separated water was passed under controlled pressure of 5.27 kg/sq.cm using pump to a reverse osmosis unit (9) to obtain pure water and the brine water was rejected. The reverse osmosis unit comprises commercially available composite polyamide membrane (made by Ion exchange ltd). The flow rate of water into the membrane unit was 30 to 100 times more than rate of product water (i.e. cross flow). The pressure applied at the outlet (10) of the reveres osmosis unit (9) by vacuum pump was 50, 100, 150, 200, 300 and 400 mm respectively. The same experiment was repeated without applying pressure at the outlet (10) of the reverse osmosis unit (9). The observed marked increase in flux of the water without affecting separation is shown in table 3. Table 3: % Increase in flux of 200 ppm NaCl solution Applied Pressure: 5.27 kg/sq.cm Pressureapplied at theoutlet (10) mmof Hg Flux in lit/day % Increase in Flux % Salt Rejection 0 216.0 — 98.22 50 227.5 5.32 97.84 100 233.3 8.00 98.22 150 239.0 10.65 98.47 200 244.8 13.33 98.22 300 250.6 16.02 98.22 400 259.2 20.00 98.47 Above results indicate that the flux of water was increased to 20.0% over initial value at no vacuum without affecting the salt rejection. 12 Example 4 The process was carried out according to the example 3 except by using 400 ppm sodium chloride solution. The % increased in the flux is shown in the Table 4. Table 4: % Increase in the flux of 400 ppm NaCl solution. Applied Pressure: 5.27 kg/sq.cm5.27 kg/sq.cm Pressureapplied at theoutlet (10) mmof Hg Flux in lit/day % Increase in Flux % Salt Rejection 0 195.8 — 97.84 50 204.5 4.44 97.77 100 210.2 7.35 97.96 150 213.1 8.84 98.03 200 224.6 14.71 97.84 300 230.4 17.67 97.84 400 236.2 20.63 97.84 Table 4 shows the flux was increased to 20.63% maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection. Example 5: The process was carried out according to the example 3 except by using 600 ppm sodium chloride solution. The % increased in the flux is shown in the Table 5. Table 5: % Increase in the flux of 600 ppm NaCl solution. Applied Pressure: 5.27 kg/sq.cm Pressureapplied at theoutlet (10) mmof Hg Flux in lit/day % Increase in Flux % Salt Rejection 0 187.2 — 97.58 50 195.8 4.59 97.46 100 204.5 9.24 97.54 150 210.2 12.29 97.29 200 216.0 15.38 97.66 300 221.7 18.43 97.58 400 233.3 24.63 97.63 Table 5 shows the flux was increased to 24.63% maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection. Example 6 The process was carried out according to the example 3 except by using 800 ppm sodium chloride solution. The % increased in the flux is shown in the Table 6. Table 6: % Increase in the flux of 800 ppm NaCl solution. Applied Pressure: 5.27 kg/sq.cm Pressure Flux in % Increase in % Salt applied at the lit/day Flux Rejection outlet (10) mm of Hg 0 178.6 ---- 97.58 50 187.2 4.82 97.55 100 192..9 8.01 97.49 150 198.7 11.25 97.52 200 204.5 14.50 97.46 300 213.1 19.32 97.42 400 218.9 22.56 97.49 Table 6 shows the flux was increased to 22.56% maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection. Example 7 The process was carried out according to the example 3 except by using 1000 ppm sodium chloride solution. The % increased in the flux is shown in the Table 7. Table 7: % Increase in the flux of 1000 ppm NaCl solution. Applied Pressure: 5.27 kg/sq.cm Pressure Flux in % Increase in % Salt applied at the lit/day Flux Rejection outlet (10) mm of Hg 0 161.3 — 96.82 14 50 169.9 5.33 96.63 100 175.7 8.93 96.56 150 178.6 10.73 96.56 200 184.3 14.26 96.63 300 195.8 21.39 96.44 400 204.5 26.78 96.37 Table 7 shows the flux was increased to 26.78% maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection. Example 8 The process was carried out according to the example 3 except by using 1200 ppm sodium chloride solution. The % increased in the flux is shown in the Table 8. Table 8: % Increase in the flux of 1200 ppm NaCl solution. Applied Pressure . 5.27kg/sq.cm Pressureapplied at theoutlet (10) mmof Hg Flux in lit/day % Increase in Flux % Salt Rejection 0 155.5 — 96.24 50 161.3 3.73 96.13 100 169.9 9.26 96.13 150 172.8 11.13 96.08 200 178.6 14.86 96.08 300 190.1 22.25 96.13 400 192.9 24.05 96.08 Table 8 shows the flux was increased to 24.05% maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection. Example 9 The process was carried out according to the example 3 except by using 1400 ppm sodium chloride solution. The % increased in the flux is shown in the Table 9. 15 Table 9: % Increase in the flux of 1400 ppm NaCl solution. Applied Pressure: 5.27 kg/sq.cm Pressureapplied at theoutlet (10) mmof Hg Flux in lit/day % Increase in Flux % Salt Rejection 0 118.1 — 96.18 50 129.6 9.74 96.14 100 138.2 17.02 96.23 150 146.9 24.39 96.14 200 155.5 31.67 96.05 300 169.9 43.86 96.00 400 181.4 53.60 96.14 Table 9 shows the flux was increased to 53.60% maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection. Example 10 The process was carried out according to the example 3 except by using 1600 ppm sodium chloride solution. The % increased in the flux is shown in the Table 10. Table 10: % Increase in the flux of 1600 ppm NaCl solution. Applied Pressure 5.27 kg/sq.cm Pressureapplied at theoutlet (10) mmof Hg Flux inlit/day % Increase in Flux % Salt Rejection 0 109.4 — 95.94 50 118.1 7.95 95.79 100 123.8 13.16 96.02 150 129.6 18.46 95.87 200 138.2 26.33 95.94 300 146.9 34.28 96.02 400 155.5 42.14 96.02 Table 10 shows the flux was increased to 42.14 % maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection. 16 Example 11 The process was carried out according to the example 3 except by using 1800 ppm sodium chloride solution. The % increased in the flux is shown in the Table 11. Table 11:% Increase in the flux of 1800 ppm NaCl solution. Applied Pressure: 5.27 kg/sq.cm: 5.27kg/sq.cm Pressureapplied at theoutlet (10) mmof Hg Flux in lit/day % Increase in Flux % Salt Rejection 0 86.4 — 96.04 50 92.2 6.71 96.04 100 100.8 16.67 95.97 150 109.4 26.62 96.11 200 120.9 39.93 96.11 300 132.5 53.36 96.11 400 146.9 70.02 96.18 Table 11 shows the flux was increased to 70.02 % maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection. Example 12 The process was carried out according to the example 3 except by using 2000 ppm sodium chloride solution. The % increased in the flux is shown in the Table 12. Table 12: % Increase in the flux of 2000 ppm NaCl solution. Applied Pressure 5.27 kg/sq.cm Pressureapplied at theoutlet (10) mmof Hg Flux in lit/day % Increase in Flux % Salt Rejection 0 86.4 — 95.93 50 97.9 13.31 95.93 100 106.6 23.38 95.93 150 115.2 33.33 95.87 200 120.9 39.93 95.87 300 135.4 56.71 95.87 17 400 144.0 66.67 95.87 Table 12 shows the flux was increased to 66.67 % maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection. Example 13 The process was carried out according to the example 3 except by using 200 ppm sugar solution and sugar solution passed to the reverse osmosis membrane unit comprising composite polyamide membrane (marketed by Permionics Ltd) under pressure of 16.32 kg/sq.cm. The % increased in the flux is shown in the Table 13. Table 13: Increase in the flux of 200 ppm sugar solution. Applied Pressure: 16.32 kg/sq.cm Pressure applied atthe outlet (10) mmof Hg Flux in lit/m2.day % Increase in Flux Without 72.5 ------- With 50 mm vacuum 125.1 72.55 With 100 mm vacuum 131.2 80.97 With 150 mm vacuum 150.0 106.90 With 200 mm vacuum 152.8 110.76 With 300 mmvacuum 149.5 106.21 Table 13 shows the flux was increased to 110.76 % maximum at 200 mm applied pressure over initial flux at without vacuum. Example 14 The process was carried out according to the example 3 except by using 500 ppm sugar solution and sugar solution passed to the reverse osmosis membrane unit comprising composite polyamide membrane (marketed by Permionics Ltd) under pressure of 16.32 kg/sq.cm. The % increased in the flux is shown in the Table 14. 18 Table 14: Increase in the flux of 500 ppm sugar solution. Applied Pressure: 16.32 kg/sq.cm. Pressure applied atthe outlet (10) mmof Hg Flux in lit/m2.day % Increase in Flux Without 69.8 — With 50 mm vacuum 127.9 83.24 With 100 mm vacuum 135.6 94.27 With 150 mm vacuum 143.9 106.16 With 200 mm vacuum 130.7 87.25 With 300 mm vacuum 110.7 58.60 Table 14 shows the flux was increased to 106.16% maximum at 150 mm applied pressure over initial flux at without vacuum. Example 15 The process was carried out according to the example 3 except by using 1000 ppm sugar solution and sugar solution passed to the reverse osmosis membrane unit comprising composite polyamide membrane (marketed by Permionics Ltd) under pressure of 16.32 kg/sq.cm. The % increased in the flux is shown in the Table 15. Table 15: Increase in the flux of 1000 ppm sugar solution. Applied Pressure: 16.32 kg/sq.cm Pressure applied at Flux in lit/m2.day % Increase in Flux the outlet (10) mm of Hg Without 56.5 --------- Vacuum With 50 mm 137.3 143.01 Vacuum With 100 mm 122.9 117.52 19 vacuum With 150 mm 104.1 84.25 vacuum With 200 mm 100.8 78.41 vacuum With 300 mm 89.1 57.70 vacuum Table 15 shows the flux was increased to 143.01% maximum at 50 mm applied pressure over initial flux at without vacuum. Example 16 The process was carried out according to the example 3 except by using 1500 ppm sugar solution and sugar solution passed to the reverse osmosis membrane unit comprising composite polyamide membrane (marketed by Permionics Ltd) under pressure of 16.32 kg/sq.cm. The % increased in the flux is shown in the Table 16. Table 16: Increase in the flux of 1500 ppm sugar solution. Applied Pressure: 16.32 kg/sq.cm Pressure applied atthe outlet (10) mmof Hg Flux in lit/m2.day % Increase in Flux Without 91.4 — vacuum With 50 mm 157.8 72.65 vacuum With 100 mm 139.5 52.63 vacuum With 150 mm 139.0 52.08 vacuum With 200 mm 134.5 47.16 vacuum With 300 mm 122.9 34.46 vacuum Table 16 shows the flux was increased to 72.65 % maximum at 50 mm applied pressure over initial flux at without vacuum without affecting salt rejection 20 Example 17 Pure water permeability of the reverse osmosis membrane of composite polyamide (marketed by Permionics ltd) used in the examples 13 to 16 was tested at various values of vacuum applied. The experiment was carried out according to the example 3 except the pure water was passed through the reverse osmosis membrane unit (9) under pressure of 16.32 kg/sq.cm. The results are shown in table 17. Table 17: Pure Water Permeability Applied Pressure: 16.32 kg/sq.cm. Pressure applied atthe outlet (10) mmof Hg Flux in lit/m2.day % Increase in Flux Without Vacuum 1605.5 ~ With 50 mm vacuum 1743.9 8.62 With 100 mm vacuum 1882.4 17.22 With 150 mm vacuum 1993.1 24.14 With 200 mm vacuum 2076.1 29.31 With 300 mm vacuum 2297.6 43.10 Example 18 The process was carried out according to the example 3 except by using 1000 ppm sodium chloride solution and passed the solution to the membrane unit (9) comprising ultrafiltration membrane of composite polyamide under pressure of 6.12 kg/sq.cm. The % increased in the flux is shown in the Table 18. Table 18: Increase in the flux of 100C ) ppm sodium chloride solution. Applied Pressure: 6.12 kg/sq.cm Pressure applied Flux in % Increase % Salt at the outlet (10) lit/day in Flux Rejection mm of Hg 21 0 238.06 ------- 61.25 50 380.62 59.88 60.00 100 336.33 41.28 60.00 200 334.95 40.70 61.25 300 332.18 39.54 61.25 Table 18 shows the flux was increased to 59.88 % maximum at 50 mm applied pressure over initial flux at without vacuum without affecting salt rejection Example 19 The process was carried out according to the example 3 except by using 1000 ppm sodium chloride solution and passed the solution to the membrane unit (9) comprising ultrafiltration membrane of composite polyamide under pressure of 8.16 kg/sq.cm. The % increased in the flux is shown in the Table 19. Table 19: Increase in the flux of 100 ppm sodium chloride solution. Applied Pressure: 8.16 kg/sq.cm. 8.16 kg/sq.cm Pressure appliedat the outlet (10)mm of Hg Flux in lit/day % Increase in Flux % Salt Rejection 0 316.96 — 60.00 50 424.91 34.06 60.00 100 362.63 14.41 60.00 200 361.24 13.97 61.25 300 361.24 13.97 60.00 Table 19 shows the flux was increased to 34.06% maximum at 50 mm applied pressure over initial flux at without vacuum without affecting salt rejection Example 20 The process was carried out according to the example 3 except by using 1000 ppm sodium chloride solution and passed the solution to the membrane unit (9) comprising ultrafiltration membrane of composite polyamide under pressure of 10.20 kg/sq.cm. The % increased in the flux is shown in the Table 20. 22 Table 20: Increase in the flux of 1000 ppm sodium chloride solution Applied Pressure: 10.20 kg/sq.cm). 0.20 kg/sq.cm Pressure appliedat the outlet (10)mm of Hg Flux in lit/day % Increase in Flux % Salt Rejection 0 325.6 — 61.25 50 437.37 34.47 62.50 100 387.54 19.15 62.50 200 386.16 18.72 61.25 300 391.69 20.42 62.50 Table 20 shows the flux was increased to 34.47% maximum at 50 mm applied pressure over initial flux at without vacuum without affecting salt rejection. Example 21 The process was carried out according to the example 3 except by using 1000 ppm sodium chloride solution and passed the solution to the membrane unit (9) comprising nanofiltration membrane of composite polyamide under pressure of 8.16 kg/sq.cm. The % increased in the flux is shown in the Table 21. Table 21: Increase in the flux of 1000 ppm sodium chloride solution. Applied Pressure: 8.16 kg/sq.cm8.16kg/sq.cm Pressureapplied at theoutlet (10) mmof Hg Flux inlit/day % Increase in Flux % Salt Rejection 0 661.59 — 87.50 50 906.57 37.03 87.50 100 898.27 35.77 87.50 150 842.91 27.41 87.50 200 838.75 26.78 87.50 300 812.46 22.80 87.50 Table 21 shows the flux was increased to 37.03 % maximum at 50 mm applied pressure over initial flux at without vacuum without affecting salt rejection 23 Example 22 The process was carried out according to the example 3 except by using 1000 ppm sodium chloride solution and passed the solution to the membrane unit (9) comprising nanofiltration membrane of composite polyamide under pressure of 12,24 kg/sq.cm. The % increased in the flux is shown in the Table 22. Table 22: Increase in the flux of 1000 ppm sodium chloride solution. Applied Pressure: 12.24 kg/sq.cm Pressureapplied at theoutlet (10) mmof Hg Flux in lit/day % Increase in Flux % Salt Rejection 0 1177.58 — 87.50 50 1513.08 28.49 87.50 100 1338.68 13.68 87.50 150 1330.38 12.98 87.50 200 1305.47 10.86 87.50 300 1283.87 9.03 87.50 Table 22 shows the flux was increased to 28.49% maximum at 50 mm applied pressure over initial flux at without vacuum without affecting salt rejection. Example 23 The process was carried out according to the example 3 except by using 1000 ppm sodium chloride solution and passed the solution to the membrane unit (9) comprising nanofiltration membrane of composite polyamide under pressure of 16.32 kg/sq.cm. The % increased in the flux is shown in the Table 23. Table 22: Increase in the flux of 1000 ppm sodium chloride solution. Applied Pressure: 12.24 kg/sq.cm Vacuum in mm of Hg Flux inlit/day % Increase in Flux % Salt Rejection 0 1531.35 — 87.50 50 1903.39 24.29 87.50 100 1921.66 25.49 87.50 24 150 1978.13 29.18 87.50 200 1910.03 24.73 87.50 300 1823.67 19.09 87.50 Table 23 shows the flux was increased to 29.18% maximum at 150 mm applied pressure over initial flux at without vacuum without affecting salt rejection 25 I claim: 1. A process for improving flux of a liquid in a separation technique by using membranes; the process comprising vacuumising a outlet (10) of a membrane unit (9) on a product side in the range of 10 mm to 700 mm Hg by applying a vacuum pump (14) at the outlet (10) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and a reservoir (13) depending on a feed temperature of a liquid which is being below the boiling point of the liquid being separated. 2. A process for improving flux of a liquid in separation technique by using membranes, the process comprising passing a liquid from a outlet (2) of a liquid supply (1) at the controlled rate through a fluid communication (3) and a inlet (4) to a activated carbon unit (5) to filter the liquid and remove odoriferous material; passing the separated liquid from a outlet (6) of the activated carbon unit (5) under controlled pressure using pump through a fluid communication (7) and a inlet (8) to a membrane unit (9) to obtain pure liquid and reject the brine liquid; passing the pure liquid from a outlet (10) of the membrane unit through a fluid communication (11) and a inlet (12) to a reservoir (13) characterized in that the outlet (10) of the membrane unit (9) being vacuumised in the range of 10 to 700 mm Hg by applying a vacuum pump (14) at the outlet (10) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) depending on a feed temperature of the liquid which is being below the boiling point of the liquid, to increase the flux of the liquid. 3. The process as claimed in claim 1 or 2, wherein the membranes selected from ultrafiltration membrane, nanofiltration membrane or reverse osmosis membrane. 4. The process as claimed in claimed in claim 1 or 2, wherein the vacuum at the outlet (10) of the membrane unit (9) is in the range of 50-400 mm Hg. 5. The process as claimed in claim 1 or 2, wherein the vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) is 0.01 meters to 9 meters of water column. 6. The process as claimed in claim 1 or 2, wherein the flux of the liquid is improved in the range of 20 % to 90 % without affecting the salt rejection. 7. The process as cliamed in claim 1 or 2, wherein the feed temperature of the liquid is in the range of 0-40°C. 8. A device for improving a flux of a liquid; the device comprising a liquid supply (1), an activated carbon (charcoal) unit (5), a membrane unit (9) and a reservoir 26 (13); each unit including reservoir is provided with inlets and outlets; a inlet (4) of the activated carbon unit (5) being in a fluid communication (3) with a outlet (2) of the liquid supply (1), a inlet (8) of the membrane unit (9) is in a fluid communication (7) with a outlet (6) of the activated carbon unit (5), a inlet (12) of the reservoir (13) being in a fluid communication (11) with a outlet (10) of the membrane unit (9) characterized in that the outlet (10) of the membrane unit (9) being vacuumised on product side in the range of 10 mm to 700 mm Hg by applying a vacuum pump (14) at the outlet (10) of the membrane unit (9) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) depending upon the feed temperature of the liquid, which is being below the boiling point of the liquid, to achieve high flux of the liquid. 9. The device as claimed in claim 8, wherein the membrane used in the membrane unit (9) is selected from ultrafiltration membrane, nanofiltration membrane or reverse osmosis membrane. 10. The device as claimed in claim 8, wherein the preferred vacuum at the outlet (10) of the membrane unit (9) is in the range of 50-300 mm Hg. 11. The device as claimed in claim 8, wherein vertical distance between the outlet of the reverse osmosis unit and the reservoir is 0.01 meters to 9 meters of water column. 12. The device as claimed in claim 8, wherein the flux of the liquid is improved in the range of 20 % to 90% without affecting the salt rejection. 13. The device as cliamed in claim 8, wherein the feed temperature of the liquid is in the range of 0-40°C. 14. Use of the process and the device as claimed in any one of claims 1 to 15 to purify the water and to increase concentration of sugars in sugar cane juice in sugar industry by application of vacuum on the permeate side. Dated this 6th day of October 2005 Prof. Vinod Chintamani Malshe Applicant 27 Abstract: A process for improving flux of a liquid in separation technique by using membranes, the process comprising passing a liquid from a outlet (2) of a liquid supply (1) at the controlled rate through a fluid communication (3) and a inlet (4) to a activated carbon unit (5) to filter the liquid and remove odoriferous material; passing the filtered liquid from a outlet (6) of the activated carbon unit (5) under controlled pressure using pump through a fluid communication (7) and an inlet (8) to a membrane unit (9) to obtain pure liquid and reject the brine liquid; passing the pure liquid from a outlet (10) of the membrane unit through a fluid communication (11) and an inlet (12) to a reservoir (12) characterized in that the outlet (10) of the membrane unit (9) being vacuumised in the range of 10 to 700 mm Hg by applying vacuum pump (14) at the outlet (10) or by increasing vertical distance between outlet (10) of the membrane unit (9) and reservoir (13) depending on the feed temperature of the liquid which being below the boiling point of the liquid, to increasing flux of liquid is disclosed. A device for improving the flux of the liquid is also disclosed. Its use in water purification and increasing concentration of sugars in sugar cane juice in sugar industry is also disclosed. 28

Full Text

FORM 2
THE PATENT ACT 1970
(39 of 1970) & The Patents Rules, 2003

COMPLETE SPECIFICATION
(See section 10 and rule 13)
1. TITLE OF THE INVENTION: A process for improving flux of liquid
2 APPLICANT
(a) Name : Malshe Vinod Chintamani
(b) Nationality : Indian
(c) Address : 1, Staff Quarters, UDCT Campus, Matunga,
Mumbai - 400 019, Maharashtra, India
3. INVENTORS
(a) Name : Malshe, Vinod Chintamani
(b) Nationality Indian
(c) Address 1, Staff Quarters, UDCT Campus, Matunga,
Mumbai - 400 019. Maharashtra, India
(a) Name Damle, Aditi Sharad
(b)Nationality : Indian
(c) Address : 1, Staff Quarters, UDCT Campus, Matunga,
Mumbai - 400 019. Maharashtra, India
3. PREAMBLE TO THE DESCRIPTION
The following specification particularly describes the invention and the manner in
which it is to be performed.

Technical Field:
The present invention relates to a process for improving flux of liquid in separation
technique using membranes.
The present invention also relates to a device, which improves the flux of a liquid in
separation technique using membranes.
The present invention relates to improving the flux of a liquid without sacrificing
separation of ultrafiltration, nanofiltration and reverse osmosis devices by activating the
finer pores for home or industrial, municipal use like water purification system and sugar
purification, etc.
The present invention relates to use of the above process and device in water purification,
sugar purification and the like end application.
Background and Prior Art:
Water is the most required commodity for homes and industry. More than 98% of the water available on earth is seawater, which is unfit for human consumption. Most of the fresh water on the surface of earth is either having high total dissolved solids (TDS) or bacterial contamination and needs to be purified. Of the various methods such as multiple effect evaporation, ion exchange and reverse osmosis available, the last method is the most preferred because it saves chemicals and energy. The water concentrated with minerals formed in the reverse osmosis can be simply discharged to the starting body of water.
In the modern medically and scientifically advanced world, people are more conscious about their health and improve and maintain the quality of drinking water by removing undesired salts and minerals. In household as well as commercial reverse osmosis (RO) plant; an active carbon (charcoal) unit is utilized as filter and an adsorbant to remove elemental chlorine and organic impurities. Charcoal removes odoriferous and colouring materials contained in water.
Reverse osmosis, a purification technique based on membrane technology, became commercially viable in the 1970's and has become central technology in high purity water processing.
Today, state of the art industrial or household high purity water systems utilize some or all the technologies like pretreatment, sand filtration, carbon treatment, softening, reverse osmosis, deionization, UV treatment, filtration in combination to provide water that approaches the theoretical ideal for pure water.
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Stage I: Fine filtration to remove the suspended solids to a very low level defined by silt density index. This operation is carried out by either sand filters or cartridge filters involving various materials for preparation of cartridges. This includes fibres of polypropylene, polyester, glass or stainless steel. Disinfection of the water is carried out with ozonation, chlorination, bromination, ultraviolet light and the residual oxidizing agent such as chlorine and organics are removed with activated Carbon, which also removes organic matter and chemical smell.
Stage II: Cellulose acetate or TFC (Thin Film Composite) Polyamide Membrane is used to remove the dissolved salts. The membranes also remove organic matters, germs, bacteria, virus, compound metals and harmful chemicals such as residues of pesticides. The pure water is collected at the end of stage II at atmospheric pressure.
In the separation of water, if the layer of pure water is removed by the application of pressure, the salts gets concentrated on the surface and have to move away to the bulk by the process of diffusion. This effectively increases osmotic pressure of the solution very close to membrane surface. Thus the external pressure is substantially neutralized by osmotic pressure of concentrated salts present next to pure water layer and available force for pushing water across the pore is represented by "Applied pressure-Osmotic pressure at the interface". Therefore from the principle of hydrostatics, if one compares flow rate of salt solution across a membrane with the same flow rate of pure water (Pure Water
3

Permeability or PWP) across the membrane, the difference in applied pressure in the two cases would represent osmotic pressure of that solution on the interface.
Thus the net driving force in a RO process is the difference of pressure between the applied pressure and the osmotic pressure at the interface. Higher the salt content of the water, more is the osmotic pressure at the interface for a given flux and thus lower is the flux. If one attempts to draw more product by applying higher pressure, more water does get out of the membrane but due to proportional rise in the osmotic pressure the net effect is very low. A membrane has pores of various dimensions on the surface. The separation takes place by adsorption of pure water on the surface and the dissolved salts are repelled or negatively adsorbed on the interface. Thus more are the dissolved solid, higher is the osmotic pressure at the interface and thus lower is the flux. Thus in a RO process, the recovery of water is a direct function of the dissolved salts. Higher the dissolved salts, lower is the recovery. Thus in a typical sea water membrane operation, the water is required to be pushed at a very high pressure of about 70 kg/ cm .Of this water only a small portion, less than 30%, can be recovered and the balance has to be discarded. Thus, the effort made in pretreating the large quantity of water is wasted. Efforts to improve the recovery of the water beyond this require modifying the entire membrane product to suit high pressure requirement thus increasing the hardware cost disproportionately and also increasing the requirement of the pumping energy to the membrane.
Objects
An object of the invention is to provide a process for achieving high flux of a liquid
without significant difference in separation by activating even the smallest of the pores
that are not active due to the low pressure, available at the interface.
Another object of the invention is to provide a process for improving flux of a liquid in the
separation technique using a membrane.
Another object of the invention is to provide a process, which provides a vacuum on the
product side of the membrane; thus pure water layer is collected with much ease (ie. Flux
is increased without any decrease in salt rejection property).
Yet another object of the invention is to provide a device for improving the flux of a liquid
in the separation technique using a membrane.
Yet another object of the invention is to provide a device, which provides a vacuum on the
product side of the membrane; thus pure water layer is collected with much ease (ie. Flux
is increased without any decrease in salt rejection property).
Yet another object the invention is to provide a use of the above process and device for
water purification.
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Yet another object of the invention is to provide a use of the above process and device for
sugar purification.
Yet another object of the invention is to provide a water purification process with the
improved flux of water without affecting a salt rejection.
Yet another object of the present invention is to provide a water purification device for
improving the flux of water without affecting the salt rejection.
Detailed Description:
According to the present invention there is provided a process for improving flux of a liquid in a separation technique by using membranes, the process comprising vacuumising a outlet (10) of a membrane unit (9) on a product side in the range of 10 mm to 700 mm Hg by applying a vacuum pump (14) at the outlet (10) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and a reservoir (13) depending on a feed temperature of a liquid which is being below the boiling point of the liquid being separated.
According to the present invention there is provided a process for improving flux of a liquid in separation technique by using membranes, the process comprising passing a liquid from a outlet (2) of a liquid supply (1) at the controlled rate through a fluid communication (3) and a inlet (4) to a activated carbon unit (5) to filter the liquid and remove odoriferous material; passing the separated liquid from a outlet (6) of the activated carbon unit (5) under controlled pressure using pump through a fluid communication (7) and a inlet (8) to a membrane unit (9) to obtain pure liquid and reject the brine liquid; passing the pure liquid from a outlet (10) of the membrane unit through a fluid communication (11) and a inlet (12) to a reservoir (13) characterized in that the outlet (10) of the membrane unit (9) being vacuumised in the range of 10 to 700 mm Hg by applying a vacuum pump (14) at the outlet (10) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) depending on a feed temperature of the liquid which is being below the boiling point of the liquid, to increase the flux of the liquid.
According to the present invention there is provided a device for improving a flux of a liquid, the device comprising a liquid supply (1), an activated carbon (charcoal) unit (5), a membrane unit (9) and a reservoir (13); each unit including reservoir is provided with inlets and outlets; a inlet (4) of the activated carbon unit (5) being in a fluid communication (3) with a outlet (2) of the liquid supply (1), a inlet (8) of the membrane unit (9) is in a fluid communication (7) with a outlet (6) of the activated carbon unit (5), a
5

inlet (12) of the reservoir (13) being in a fluid communication (11) with a outlet (10) of the membrane unit (9) characterized in that the outlet (10) of the membrane unit (9) being vacuumised on product side in the range of 10 mm to 700 mm Hg by applying a vacuum pump (14) at the outlet (10) of the membrane unit (9) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) depending upon the feed temperature of the liquid, which is being below the boiling point of the liquid, to achieve high flux of the liquid.
Preferably the membrane used in the membrane unit (9) is selected from ultrafiltration membrane, nanofiltration membrane or reverse osmosis membrane. More preferably the membranes used are cellulose acetate or composite polyamide or polysulfone or any composite membrane of suitable size and shape and has flux rate 10 m3 after applying 10 kg/cm 2 pressure. Preferably the vacuum at the outlet (10) of the membrane unit (9) is in the range of 50-400 mm Hg. Preferably the vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) is in the range of 0.01 meters to 9 meters of water column. The flux of the liquid is improved in the range of 20 % to 90 %. Preferably the feed temperature of the liquid is in the range of 2 - 40°C. Higher vacuum is applied at the lower feed water temperature.
The vacuum can be applied with the help of a vacuum pump or by increasing a vertical distance between the outlet of the membrane unit and the storage tank or reservoir using barometric leg. Second alternative has an advantage of inbuilt facility for creating vacuum without mechanical work. The preferred vacuum at the outlet (10) of the membrane unit (9) is 400 mm Hg or the preferred distance between the outlet (10) of the membrane unit (9) and the reservoir (13) is 4 meter. It is easily possible to raise the entire apparatus to a higher elevation in an existing installation and it is possible to provide the facility for a new installation.
The improvement in flux is more in the case of higher salt concentration compared to lower ones particularly at higher applied pressure.
According to the present invention there is provided use of the process and the device to purify the water and to increase concentration of sugars in sugar cane juice in sugar industry by application of vacuum on the permeate side.
According to the present invention there is provided a use of the above device to purify water, the device comprising a water supply (1), an activated carbon (charcoal) unit (5), a membrane unit (9) and a reservoir (13); each unit including the reservoir is provided with inlets and outlets; a inlet (4) of the activated carbon unit (5) being in a fluid communication (3) with a outlet (2) of the liquid supply (1), a inlet (8) of the membrane unit (9) is in a fluid communication (7) with a outlet (6) of the activated carbon unit (5), a
6

inlet (12) of the reservoir (13) being in a fluid communication (11) with a outlet (10) of the membrane unit (9) characterized in that the outlet (10) of the membrane unit (9) being vacuumised on product side in the range of 10 mm to 700 mm Hg by applying a vacuum pump (14) at the outlet (10) of the membrane unit (9) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) depending upon a feed temperature of water, which is being below the boiling point of the liquid, to achieve high flux of the water.
According to the present invention there is provided a use of the above process to purify the water, the process comprising passing a water from a outlet (2) of a water supply (1) at the controlled rate through a fluid communication (3) and a inlet (4) to a activated carbon unit (5) to filter the water and remove odoriferous material; passing the filtered water from a outlet (6) of the activated carbon unit (5) under controlled pressure using pump through a fluid communication (7) and a inlet (8) to a membrane unit (9) to obtain pure water and reject the brine water; passing the pure water from a outlet (10) of the membrane unit through a fluid communication (11) and a inlet (12) to a reservoir (12) characterized in that the outlet (10) of the membrane unit (9) being vacuumised in the range of 10 to 700 mm Hg by applying a vacuum pump (14) at the outlet (10) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) depending on a feed temperature of the water which being below the boiling point of the liquid, to increase flux of liquid without affecting the salt rejection.
Preferably the membrane used in the membrane unit (9) is selected from ultrafiltration membrane, nanofiltration membrane or reverse osmosis membrane. More preferably the membranes used are cellulose acetate or composite polyamide or polysulfone or any composite membrane of suitable size and shape and has flux rate 10 m3 after applying 10 kg/cm pressure. Preferably the vacuum at the outlet (10) of the membrane unit (9) is in the range of 50-400 mm Hg. Preferably the vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) is in range of 0.01 meters to 9 meters of water column. The flux of the liquid is improved in the range of 20 % to 90 % without affecting the salt rejection. Preferably the feed temperature of the water is in the range of 0 - 40°C The fluid communication means being plastic / metal pipes. The units and reservoir also are fabricated from suitable safe plastics / metals. The membrane unit is also provided with an outlet for removing urine liquid/ mineral concentrated liquid / brine liquid. The brine liquid / urine liquid is intended to apply to the liquid containing a higher concentration of undesirable ions / salts.
The invention is described with the drawing and description, which follows. Figure 2 is a schematic representation of the system.
7

Referring now to the accompanying drawing: a outlet (2) of a liquid supply (1) is connected by a fluid communication (3) to a inlet (4) of an activated carbon unit (5). The liquid is supplied to the activated carbon unit (5) under controlled rate by using valve. A outlet (6) of the activated carbon unit (5) is connected by a fluid communication (7) to a inlet (8) of a membrane unit (9). The liquid filtered through the activated carbon unit (5) is supplied under pressure to the membrane unit (9) by using a pump. The cellulose fiber filter may be held in fluid communication (7) to prevent any active carbon particle from entering the membrane unit (9). The membrane unit (9) contains ultrafiltration membrane/ nanofiltration membrane / reverse osmosis membrane, either prepared from cellulose acetate or from thin composite polysulfone or polyamide or composite membrane of suitable size and shape has flux rate 10 m3 after applying 10 kg/cm 2 pressure. A outlet (10) of the membrane unit (9) is connected by a fluid communication (11) to a inlet (12) of a reservoir (13). The membrane unit is vacuumised at the other end of the membrane towards the outlet (10) by applying a vacuum pump (14) at the outlet (10) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13). The pressure created by vacuum directly regulates the flux of the liquid and salt rejection. The pure liquid is passed through the outlet (10) into the reservoir (13). The brine liquid rejected is passed through outlet (15) of the membrane unit (10) to discharge. The reservoir (13) may have an outlet means with a suitable opening valve. The brine to permeate ratio is 10-15%.
Separation starts as soon as the membrane is brought in contact with the liquid, as flux and separation are the function of the total pore area and pore size distribution. If the layer of pure water is removed by application of pressure, the salts get concentrated on the surface and have to move away to the bulk by the process of diffusion. This effectively increases osmotic pressure of the solution very close to membrane surface. Thus the external pressure is substantially neutralized by osmotic pressure of concentrated salt present next to pure water layer and available force for pushing water across the pore is represented by "Applied pressure-Osmotic pressure at the interface". In the present invention we applied pressure on both the side of the membrane to overcome the osmotic pressure and thereby achieved high rate flow of water. The present method and device for water purification give much higher flux for the same applied pressure without significant difference in separation. Applied total pressure is very critical in the invention. High vacuum leads to boiling of water and disturbs the membrane operation.
The separation by using the membranes is a tangential flow process where the feed stream splits into treated water (called permeate or product water) and wastewater (called reject or concentrate water) as it is processed. Contaminants present in the feed stream are
8

removed from water that passes through the membrane and concentrate in the water that remains behind. It is important to maintain adequate flow in the "concentrate" stream to prevent contaminants from depositing on the membranes. As the liquid temperature is reduced, the amount of product liquid produced is also reduced due to increase in liquid viscosity and the shrinkage of pores associated with temperature changes.
The membranes may require periodic cleaning and should be cleaned if the product liquid flow-rate falls to less than 50% below normal (with feed liquid composition, temperature and pressure conditions being the same). The liquid is fed with scale control polymers or additives, acid to lower the pH to prevent crystallization of carbonates, sulfates and phosphates of calcium, magnesium and strontium. The device may be furnished with various instruments and controls to permit monitoring of its operation and performance. Pressure gauges may be provided to permit monitoring of the membrane feed and concentrate pressures. Flow meters may be provided for monitoring the product and reject stream flow rates. Conductivity monitor may be provided to measure the percent of ionized solids removed by the system (called percent rejection). The membrane unit may employ a pressure relief valve to prevent the unintentional back over pressurization of the membranes, which could damage the membranes. The system ranges from small stills, through to wall mounted water systems to industrial manufacturing water systems housed in their own buildings to vast desalinization plants occupying acres, providing drinking water from hard water.
Thus by using this technique, the flux of the liquid improves to 20 to 90 % without change in the separation. This is envisaged by applying vacuum at the other surface of the membrane, which essentially provides a higher driving force for the pure water that has already been separated by adsorption of pure water by the membrane surface. Thus the net difference in the pressure across the membrane is much more than just an additional pressure equal to the vacuum applied on the front side of the membrane.
The invention is further illustrated by the following examples, which should not construe the effective scope of the claims. The examples are given only to illustrate the phenomenon and are not limited to any one application.
Example 1:
Water in the form of saturated sodium chloride solution (1000 ppm) from water supply (1) was passed at the controlled rate ie at 5.27 kg/sq.cm using valve to an activated carbon unit (5) to filter the water and removed odoriferous material. The separated water was passed under controlled pressure of 6.12 kg/sq.cm, 8.16 kg/sq.cm and 10.20 kg/sq.cm
9

respectively using a pump to a reverse osmosis unit (9) to obtain pure water and the brine water was rejected. The reverse osmosis unit comprises commercially available composite polyamide membrane (made by Ion-Exchange Ltd). The flow rate of water into the membrane unit was 30 to 100 times more than rate of product water (i.e. cross flow). The pressure applied at the outlet (10) of the reveres osmosis unit (9) by vacuum pump is 50, 100, 150, 200, 300 and 400 mm respectively. The same experiment is repeated without applying pressure at the outlet (10) of the reverse osmosis unit (9) ie. at atmospheric pressure. The observed marked increase in flux of the water without affecting separation is shown in table 1.

Table 1: Increase in flux for 1000 ppm NaCl solution
Pressure Pressure applied at the inlet of the membrane unit (9)
applied at the outlet (10) mm of Hg 6.12 Kg/sq.cm 8.16 Kg/sq.cm 10.20 Kg/sq.cm
Flux In lmd %Increasein flux %Saltrejection Flux In lmd %Increasein flux %Saltrejection Flux In lmd /oIncrease in flux %Saltrejection
Without vacuum 193.49 ™ 87.02 268.23 ™ 94.91 369.55 " 96.44
50 mm Hg 353.77 82.84 91.86 361.25 34.68 94.15 481.66 30.34 96.18
100 mm Hg 306.43 58.37 90.33 377.02 40.56 93.90 494.12 33.71 96.18
150 mm Hg 248.30 28.33 93.64 383.66 43.03 95.42 514.88 39.33 96.69
200 mm Hg 235.02 21.46 93.13 332.18 23.84 95.68 528.17 42.92 96.44
300 mm Hg 238.34 23.18 95.42 330.52 23.22 93.64 519.86 40.67 96.44
400 mm Hg 233.36 20.61 93.64 332.18 23.84 95.93 514.88 39.33 96.69
10

The table 1 indicates the flux of the water was improved without affecting the salt rejection. The flux of the water was increased with the increase in the pressure applied at the outlet (10) of the reverse osmosis unit (9).
Example 2
Pure water permeability of the commercially available composite polyamide membrane (made by Ion Exchange ltd) was detected by applying pressure at the outlet (10) of the reverse osmosis membrane unit (9). The flux of the pure water should always be higher than the flux of the salt solution at any pressure that acts as a positive control for the method. Pure water was passed under controlled pressure of 5.27 kg/sq.cm using pump to a reverse osmosis unit (9). The reverse osmosis unit comprises commercially available composite polyamide membrane (made by Ion exchange ltd). The pressure applied at the outlet (10) of the reveres osmosis unit (9) by vacuum pump was 50, 100, 150, 200, 300 and 400 mm respectively. The same experiment was repeated without applying the pressure at the outlet (10) of the reverse osmosis unit (9). The observed marked increase in flux of the pure water is shown in table 2.

Table 2: Pure Water Permeability
Applied pressure on the membrane = 5.27 kg/sq.cm
Pressure Flux in % Increase in
applied at the lit/day Flux
Outlet
In mm of Hg
0 236.2 —
50 253.4 7.28
100 265.0 12.19
150 276.5 17.06
200 299.5 26.80
300 316.8 34.12
400 351.4 48.77
Above results of table 2 show the flux was increased with increase in applied pressure at the outlet (10). It reaches a maximum of 48.77% over initial value at atmospheric pressure (no vacuum).
Example 3:
Water in the form of saturated sodium chloride solution (200 ppm) from water supply (1) was passed at the controlled rate ie at 5.27 kg/sq.cm using valve to an activated carbon
11

unit (5) to filter the water and removed odoriferous material. The separated water was passed under controlled pressure of 5.27 kg/sq.cm using pump to a reverse osmosis unit
(9) to obtain pure water and the brine water was rejected. The reverse osmosis unit
comprises commercially available composite polyamide membrane (made by Ion
exchange ltd). The flow rate of water into the membrane unit was 30 to 100 times more
than rate of product water (i.e. cross flow). The pressure applied at the outlet (10) of the
reveres osmosis unit (9) by vacuum pump was 50, 100, 150, 200, 300 and 400 mm
respectively. The same experiment was repeated without applying pressure at the outlet
(10) of the reverse osmosis unit (9). The observed marked increase in flux of the water
without affecting separation is shown in table 3.
Table 3: % Increase in flux of 200 ppm NaCl solution

Applied Pressure: 5.27 kg/sq.cm
Pressureapplied at theoutlet (10) mmof Hg Flux in lit/day % Increase in Flux % Salt Rejection
0 216.0 — 98.22
50 227.5 5.32 97.84
100 233.3 8.00 98.22
150 239.0 10.65 98.47
200 244.8 13.33 98.22
300 250.6 16.02 98.22
400 259.2 20.00 98.47
Above results indicate that the flux of water was increased to 20.0% over initial value at no vacuum without affecting the salt rejection.
12

Example 4
The process was carried out according to the example 3 except by using 400 ppm sodium chloride solution. The % increased in the flux is shown in the Table 4.
Table 4: % Increase in the flux of 400 ppm NaCl solution.

Applied Pressure: 5.27 kg/sq.cm5.27 kg/sq.cm
Pressureapplied at theoutlet (10) mmof Hg Flux in lit/day % Increase in Flux % Salt Rejection
0 195.8 — 97.84
50 204.5 4.44 97.77
100 210.2 7.35 97.96
150 213.1 8.84 98.03
200 224.6 14.71 97.84
300 230.4 17.67 97.84
400 236.2 20.63 97.84
Table 4 shows the flux was increased to 20.63% maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection.
Example 5:
The process was carried out according to the example 3 except by using 600 ppm sodium chloride solution. The % increased in the flux is shown in the Table 5.
Table 5: % Increase in the flux of 600 ppm NaCl solution.

Applied Pressure: 5.27 kg/sq.cm
Pressureapplied at theoutlet (10) mmof Hg Flux in lit/day % Increase in Flux % Salt Rejection
0 187.2 — 97.58
50 195.8 4.59 97.46
100 204.5 9.24 97.54
150 210.2 12.29 97.29
200 216.0 15.38 97.66

300 221.7 18.43 97.58
400 233.3 24.63 97.63
Table 5 shows the flux was increased to 24.63% maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection.
Example 6
The process was carried out according to the example 3 except by using 800 ppm sodium chloride solution. The % increased in the flux is shown in the Table 6.
Table 6: % Increase in the flux of 800 ppm NaCl solution.
Applied Pressure: 5.27 kg/sq.cm
Pressure Flux in % Increase in % Salt
applied at the lit/day Flux Rejection
outlet (10) mm
of Hg
0 178.6 ---- 97.58
50 187.2 4.82 97.55
100 192..9 8.01 97.49
150 198.7 11.25 97.52
200 204.5 14.50 97.46
300 213.1 19.32 97.42
400 218.9 22.56 97.49
Table 6 shows the flux was increased to 22.56% maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection.
Example 7
The process was carried out according to the example 3 except by using 1000 ppm sodium chloride solution. The % increased in the flux is shown in the Table 7.
Table 7: % Increase in the flux of 1000 ppm NaCl solution.
Applied Pressure: 5.27 kg/sq.cm

Pressure Flux in % Increase in % Salt
applied at the lit/day Flux Rejection
outlet (10) mm
of Hg
0 161.3 — 96.82
14

50 169.9 5.33 96.63
100 175.7 8.93 96.56
150 178.6 10.73 96.56
200 184.3 14.26 96.63
300 195.8 21.39 96.44
400 204.5 26.78 96.37
Table 7 shows the flux was increased to 26.78% maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection.
Example 8
The process was carried out according to the example 3 except by using 1200 ppm sodium chloride solution. The % increased in the flux is shown in the Table 8.
Table 8: % Increase in the flux of 1200 ppm NaCl solution.

Applied Pressure . 5.27kg/sq.cm
Pressureapplied at theoutlet (10) mmof Hg Flux in lit/day % Increase in Flux % Salt Rejection
0 155.5 — 96.24
50 161.3 3.73 96.13
100 169.9 9.26 96.13
150 172.8 11.13 96.08
200 178.6 14.86 96.08
300 190.1 22.25 96.13
400 192.9 24.05 96.08
Table 8 shows the flux was increased to 24.05% maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection.
Example 9
The process was carried out according to the example 3 except by using 1400 ppm sodium chloride solution. The % increased in the flux is shown in the Table 9.
15

Table 9: % Increase in the flux of 1400 ppm NaCl solution. Applied Pressure: 5.27 kg/sq.cm
Pressureapplied at theoutlet (10) mmof Hg Flux in lit/day % Increase in Flux % Salt Rejection
0 118.1 — 96.18
50 129.6 9.74 96.14
100 138.2 17.02 96.23
150 146.9 24.39 96.14
200 155.5 31.67 96.05
300 169.9 43.86 96.00
400 181.4 53.60 96.14
Table 9 shows the flux was increased to 53.60% maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection.
Example 10
The process was carried out according to the example 3 except by using 1600 ppm sodium chloride solution. The % increased in the flux is shown in the Table 10.
Table 10: % Increase in the flux of 1600 ppm NaCl solution.

Applied Pressure 5.27 kg/sq.cm
Pressureapplied at theoutlet (10) mmof Hg Flux inlit/day % Increase in Flux % Salt Rejection
0 109.4 — 95.94
50 118.1 7.95 95.79
100 123.8 13.16 96.02
150 129.6 18.46 95.87
200 138.2 26.33 95.94
300 146.9 34.28 96.02
400 155.5 42.14 96.02
Table 10 shows the flux was increased to 42.14 % maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection.
16

Example 11
The process was carried out according to the example 3 except by using 1800 ppm sodium chloride solution. The % increased in the flux is shown in the Table 11.
Table 11:% Increase in the flux of 1800 ppm NaCl solution.

Applied Pressure: 5.27 kg/sq.cm: 5.27kg/sq.cm
Pressureapplied at theoutlet (10) mmof Hg Flux in lit/day % Increase in Flux % Salt Rejection
0 86.4 — 96.04
50 92.2 6.71 96.04
100 100.8 16.67 95.97
150 109.4 26.62 96.11
200 120.9 39.93 96.11
300 132.5 53.36 96.11
400 146.9 70.02 96.18
Table 11 shows the flux was increased to 70.02 % maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection.
Example 12
The process was carried out according to the example 3 except by using 2000 ppm sodium chloride solution. The % increased in the flux is shown in the Table 12.
Table 12: % Increase in the flux of 2000 ppm NaCl solution.

Applied Pressure 5.27 kg/sq.cm
Pressureapplied at theoutlet (10) mmof Hg Flux in lit/day % Increase in Flux % Salt Rejection
0 86.4 — 95.93
50 97.9 13.31 95.93
100 106.6 23.38 95.93
150 115.2 33.33 95.87
200 120.9 39.93 95.87
300 135.4 56.71 95.87
17

400 144.0 66.67 95.87
Table 12 shows the flux was increased to 66.67 % maximum at 400 mm applied pressure over initial flux at without vacuum without affecting salt rejection.
Example 13
The process was carried out according to the example 3 except by using 200 ppm sugar solution and sugar solution passed to the reverse osmosis membrane unit comprising composite polyamide membrane (marketed by Permionics Ltd) under pressure of 16.32 kg/sq.cm. The % increased in the flux is shown in the Table 13.

Table 13: Increase in the flux of 200 ppm sugar solution. Applied Pressure: 16.32 kg/sq.cm
Pressure applied atthe outlet (10) mmof Hg Flux in lit/m2.day % Increase in Flux
Without 72.5 -------
With 50 mm vacuum 125.1 72.55
With 100 mm vacuum 131.2 80.97
With 150 mm vacuum 150.0 106.90
With 200 mm vacuum 152.8 110.76
With 300 mmvacuum 149.5 106.21
Table 13 shows the flux was increased to 110.76 % maximum at 200 mm applied pressure over initial flux at without vacuum.
Example 14
The process was carried out according to the example 3 except by using 500 ppm sugar solution and sugar solution passed to the reverse osmosis membrane unit comprising composite polyamide membrane (marketed by Permionics Ltd) under pressure of 16.32 kg/sq.cm. The % increased in the flux is shown in the Table 14.
18

Table 14: Increase in the flux of 500 ppm sugar solution. Applied Pressure: 16.32 kg/sq.cm.
Pressure applied atthe outlet (10) mmof Hg Flux in lit/m2.day % Increase in Flux
Without 69.8 —
With 50 mm vacuum 127.9 83.24
With 100 mm vacuum 135.6 94.27
With 150 mm vacuum 143.9 106.16
With 200 mm vacuum 130.7 87.25
With 300 mm vacuum 110.7 58.60
Table 14 shows the flux was increased to 106.16% maximum at 150 mm applied pressure over initial flux at without vacuum.
Example 15
The process was carried out according to the example 3 except by using 1000 ppm sugar solution and sugar solution passed to the reverse osmosis membrane unit comprising composite polyamide membrane (marketed by Permionics Ltd) under pressure of 16.32 kg/sq.cm. The % increased in the flux is shown in the Table 15.

Table 15: Increase in the flux of 1000 ppm sugar solution.
Applied Pressure: 16.32 kg/sq.cm
Pressure applied at Flux in lit/m2.day % Increase in Flux
the outlet (10) mm
of Hg
Without 56.5 ---------
Vacuum
With 50 mm 137.3 143.01
Vacuum
With 100 mm 122.9 117.52
19

vacuum
With 150 mm 104.1 84.25
vacuum
With 200 mm 100.8 78.41
vacuum
With 300 mm 89.1 57.70
vacuum
Table 15 shows the flux was increased to 143.01% maximum at 50 mm applied pressure over initial flux at without vacuum.
Example 16
The process was carried out according to the example 3 except by using 1500 ppm sugar solution and sugar solution passed to the reverse osmosis membrane unit comprising composite polyamide membrane (marketed by Permionics Ltd) under pressure of 16.32 kg/sq.cm. The % increased in the flux is shown in the Table 16.

Table 16: Increase in the flux of 1500 ppm sugar solution. Applied Pressure: 16.32 kg/sq.cm
Pressure applied atthe outlet (10) mmof Hg Flux in lit/m2.day % Increase in Flux
Without 91.4 —
vacuum
With 50 mm 157.8 72.65
vacuum
With 100 mm 139.5 52.63
vacuum
With 150 mm 139.0 52.08
vacuum
With 200 mm 134.5 47.16
vacuum
With 300 mm 122.9 34.46
vacuum
Table 16 shows the flux was increased to 72.65 % maximum at 50 mm applied pressure over initial flux at without vacuum without affecting salt rejection
20

Example 17
Pure water permeability of the reverse osmosis membrane of composite polyamide (marketed by Permionics ltd) used in the examples 13 to 16 was tested at various values of vacuum applied. The experiment was carried out according to the example 3 except the pure water was passed through the reverse osmosis membrane unit (9) under pressure of 16.32 kg/sq.cm. The results are shown in table 17.

Table 17: Pure Water Permeability Applied Pressure: 16.32 kg/sq.cm.
Pressure applied atthe outlet (10) mmof Hg Flux in lit/m2.day % Increase in Flux
Without Vacuum 1605.5 ~
With 50 mm vacuum 1743.9 8.62
With 100 mm vacuum 1882.4 17.22
With 150 mm vacuum 1993.1 24.14
With 200 mm vacuum 2076.1 29.31
With 300 mm vacuum 2297.6 43.10
Example 18
The process was carried out according to the example 3 except by using 1000 ppm sodium chloride solution and passed the solution to the membrane unit (9) comprising ultrafiltration membrane of composite polyamide under pressure of 6.12 kg/sq.cm. The % increased in the flux is shown in the Table 18.

Table 18: Increase in the flux of 100C ) ppm sodium chloride solution.
Applied Pressure: 6.12 kg/sq.cm
Pressure applied Flux in % Increase % Salt
at the outlet (10) lit/day in Flux Rejection
mm of Hg
21

0 238.06 ------- 61.25
50 380.62 59.88 60.00
100 336.33 41.28 60.00
200 334.95 40.70 61.25
300 332.18 39.54 61.25
Table 18 shows the flux was increased to 59.88 % maximum at 50 mm applied pressure over initial flux at without vacuum without affecting salt rejection
Example 19
The process was carried out according to the example 3 except by using 1000 ppm sodium chloride solution and passed the solution to the membrane unit (9) comprising ultrafiltration membrane of composite polyamide under pressure of 8.16 kg/sq.cm. The % increased in the flux is shown in the Table 19.

Table 19: Increase in the flux of 100 ppm sodium chloride solution. Applied Pressure: 8.16 kg/sq.cm. 8.16 kg/sq.cm
Pressure appliedat the outlet (10)mm of Hg Flux in lit/day % Increase in Flux % Salt Rejection
0 316.96 — 60.00
50 424.91 34.06 60.00
100 362.63 14.41 60.00
200 361.24 13.97 61.25
300 361.24 13.97 60.00
Table 19 shows the flux was increased to 34.06% maximum at 50 mm applied pressure over initial flux at without vacuum without affecting salt rejection
Example 20
The process was carried out according to the example 3 except by using 1000 ppm sodium chloride solution and passed the solution to the membrane unit (9) comprising ultrafiltration membrane of composite polyamide under pressure of 10.20 kg/sq.cm. The % increased in the flux is shown in the Table 20.
22

Table 20: Increase in the flux of 1000 ppm sodium chloride solution Applied Pressure: 10.20 kg/sq.cm). 0.20 kg/sq.cm
Pressure appliedat the outlet (10)mm of Hg Flux in lit/day % Increase in Flux % Salt Rejection
0 325.6 — 61.25
50 437.37 34.47 62.50
100 387.54 19.15 62.50
200 386.16 18.72 61.25
300 391.69 20.42 62.50
Table 20 shows the flux was increased to 34.47% maximum at 50 mm applied pressure over initial flux at without vacuum without affecting salt rejection.
Example 21
The process was carried out according to the example 3 except by using 1000 ppm sodium chloride solution and passed the solution to the membrane unit (9) comprising nanofiltration membrane of composite polyamide under pressure of 8.16 kg/sq.cm. The % increased in the flux is shown in the Table 21.

Table 21: Increase in the flux of 1000 ppm sodium chloride solution. Applied Pressure: 8.16 kg/sq.cm8.16kg/sq.cm
Pressureapplied at theoutlet (10) mmof Hg Flux inlit/day % Increase in Flux % Salt Rejection
0 661.59 — 87.50
50 906.57 37.03 87.50
100 898.27 35.77 87.50
150 842.91 27.41 87.50
200 838.75 26.78 87.50
300 812.46 22.80 87.50
Table 21 shows the flux was increased to 37.03 % maximum at 50 mm applied pressure over initial flux at without vacuum without affecting salt rejection
23

Example 22
The process was carried out according to the example 3 except by using 1000 ppm sodium chloride solution and passed the solution to the membrane unit (9) comprising nanofiltration membrane of composite polyamide under pressure of 12,24 kg/sq.cm. The % increased in the flux is shown in the Table 22.
Table 22: Increase in the flux of 1000 ppm sodium chloride solution.

Applied Pressure: 12.24 kg/sq.cm
Pressureapplied at theoutlet (10) mmof Hg Flux in lit/day % Increase in Flux % Salt Rejection
0 1177.58 — 87.50
50 1513.08 28.49 87.50
100 1338.68 13.68 87.50
150 1330.38 12.98 87.50
200 1305.47 10.86 87.50
300 1283.87 9.03 87.50
Table 22 shows the flux was increased to 28.49% maximum at 50 mm applied pressure over initial flux at without vacuum without affecting salt rejection.
Example 23
The process was carried out according to the example 3 except by using 1000 ppm sodium chloride solution and passed the solution to the membrane unit (9) comprising nanofiltration membrane of composite polyamide under pressure of 16.32 kg/sq.cm. The % increased in the flux is shown in the Table 23.
Table 22: Increase in the flux of 1000 ppm sodium chloride solution.

Applied Pressure: 12.24 kg/sq.cm
Vacuum in mm of Hg Flux inlit/day % Increase in Flux % Salt Rejection
0 1531.35 — 87.50
50 1903.39 24.29 87.50
100 1921.66 25.49 87.50
24

150 1978.13 29.18 87.50
200 1910.03 24.73 87.50
300 1823.67 19.09 87.50
Table 23 shows the flux was increased to 29.18% maximum at 150 mm applied pressure over initial flux at without vacuum without affecting salt rejection
25

I claim:
1. A process for improving flux of a liquid in a separation technique by using
membranes; the process comprising vacuumising a outlet (10) of a membrane unit
(9) on a product side in the range of 10 mm to 700 mm Hg by applying a vacuum
pump (14) at the outlet (10) or by increasing a vertical distance between the outlet
(10) of the membrane unit (9) and a reservoir (13) depending on a feed
temperature of a liquid which is being below the boiling point of the liquid being
separated.
2. A process for improving flux of a liquid in separation technique by using membranes, the process comprising passing a liquid from a outlet (2) of a liquid supply (1) at the controlled rate through a fluid communication (3) and a inlet (4) to a activated carbon unit (5) to filter the liquid and remove odoriferous material; passing the separated liquid from a outlet (6) of the activated carbon unit (5) under controlled pressure using pump through a fluid communication (7) and a inlet (8) to a membrane unit (9) to obtain pure liquid and reject the brine liquid; passing the pure liquid from a outlet (10) of the membrane unit through a fluid communication (11) and a inlet (12) to a reservoir (13) characterized in that the outlet (10) of the membrane unit (9) being vacuumised in the range of 10 to 700 mm Hg by applying a vacuum pump (14) at the outlet (10) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) depending on a feed temperature of the liquid which is being below the boiling point of the liquid, to increase the flux of the liquid.
3. The process as claimed in claim 1 or 2, wherein the membranes selected from ultrafiltration membrane, nanofiltration membrane or reverse osmosis membrane.
4. The process as claimed in claimed in claim 1 or 2, wherein the vacuum at the outlet (10) of the membrane unit (9) is in the range of 50-400 mm Hg.
5. The process as claimed in claim 1 or 2, wherein the vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) is 0.01 meters to 9 meters of water column.
6. The process as claimed in claim 1 or 2, wherein the flux of the liquid is improved in the range of 20 % to 90 % without affecting the salt rejection.
7. The process as cliamed in claim 1 or 2, wherein the feed temperature of the liquid is in the range of 0-40°C.
8. A device for improving a flux of a liquid; the device comprising a liquid supply (1), an activated carbon (charcoal) unit (5), a membrane unit (9) and a reservoir
26

(13); each unit including reservoir is provided with inlets and outlets; a inlet (4) of the activated carbon unit (5) being in a fluid communication (3) with a outlet (2) of the liquid supply (1), a inlet (8) of the membrane unit (9) is in a fluid communication (7) with a outlet (6) of the activated carbon unit (5), a inlet (12) of the reservoir (13) being in a fluid communication (11) with a outlet (10) of the membrane unit (9) characterized in that the outlet (10) of the membrane unit (9) being vacuumised on product side in the range of 10 mm to 700 mm Hg by applying a vacuum pump (14) at the outlet (10) of the membrane unit (9) or by increasing a vertical distance between the outlet (10) of the membrane unit (9) and the reservoir (13) depending upon the feed temperature of the liquid, which is being below the boiling point of the liquid, to achieve high flux of the liquid.
9. The device as claimed in claim 8, wherein the membrane used in the membrane unit (9) is selected from ultrafiltration membrane, nanofiltration membrane or reverse osmosis membrane.
10. The device as claimed in claim 8, wherein the preferred vacuum at the outlet (10) of the membrane unit (9) is in the range of 50-300 mm Hg.
11. The device as claimed in claim 8, wherein vertical distance between the outlet of the reverse osmosis unit and the reservoir is 0.01 meters to 9 meters of water column.
12. The device as claimed in claim 8, wherein the flux of the liquid is improved in the range of 20 % to 90% without affecting the salt rejection.
13. The device as cliamed in claim 8, wherein the feed temperature of the liquid is in the range of 0-40°C.
14. Use of the process and the device as claimed in any one of claims 1 to 15 to purify the water and to increase concentration of sugars in sugar cane juice in sugar industry by application of vacuum on the permeate side.
Dated this 6th day of October 2005

Prof. Vinod Chintamani Malshe Applicant
27

Abstract:
A process for improving flux of a liquid in separation technique by using membranes, the process comprising passing a liquid from a outlet (2) of a liquid supply (1) at the controlled rate through a fluid communication (3) and a inlet (4) to a activated carbon unit (5) to filter the liquid and remove odoriferous material; passing the filtered liquid from a outlet (6) of the activated carbon unit (5) under controlled pressure using pump through a fluid communication (7) and an inlet (8) to a membrane unit (9) to obtain pure liquid and reject the brine liquid; passing the pure liquid from a outlet (10) of the membrane unit through a fluid communication (11) and an inlet (12) to a reservoir
(12) characterized in that the outlet (10) of the membrane unit (9) being vacuumised in the range of 10 to 700 mm Hg by applying vacuum pump (14) at the outlet (10) or by increasing vertical distance between outlet (10) of the membrane unit (9) and reservoir
(13) depending on the feed temperature of the liquid which being below the boiling point of the liquid, to increasing flux of liquid is disclosed. A device for improving the flux of the liquid is also disclosed. Its use in water purification and increasing concentration of sugars in sugar cane juice in sugar industry is also disclosed.
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Documents:

1263-mum-2005-abstract(granted)-(15-2-2010).pdf

1263-mum-2005-abstract.doc

1263-mum-2005-abstract.pdf

1263-mum-2005-cancelled pages(21-12-2009).pdf

1263-MUM-2005-CLAIMS(AMENDED)-(21-12-2009).pdf

1263-mum-2005-claims(granted)-(15-2-2010).pdf

1263-mum-2005-claims.doc

1263-mum-2005-claims.pdf

1263-mum-2005-correspondence(11-4-2008).pdf

1263-MUM-2005-CORRESPONDENCE(15-2-2010).pdf

1263-mum-2005-correspondence(ipo)-(25-3-2010).pdf

1263-mum-2005-correspondence(ipo)-(27-1-2009).pdf

1263-mum-2005-correspondence-received.pdf

1263-mum-2005-description(granted)-(15-2-2010).pdf

1263-mum-2005-drawing(granted)-(15-2-2010).pdf

1263-mum-2005-drawing.pdf

1263-MUM-2005-FORM 1(21-12-2009).pdf

1263-mum-2005-form 13(11-4-2008).pdf

1263-mum-2005-form 13(15-2-2010).pdf

1263-mum-2005-form 18(11-4-2008).pdf

1263-mum-2005-form 2(granted)-(15-2-2010).pdf

1263-MUM-2005-FORM 2(TITLE PAGE)-(21-12-2009).pdf

1263-mum-2005-form 2(title page)-(granted)-(15-2-2010).pdf

1263-mum-2005-form 26(21-12-2009).pdf

1263-MUM-2005-FORM 3(21-12-2009).pdf

1263-mum-2005-form-1.pdf

1263-mum-2005-form-2.doc

1263-mum-2005-form-2.pdf

1263-mum-2005-form-3.pdf

1263-MUM-2005-REPLY TO EXAMINATION REPORT(21-12-2009).pdf

1263-mum-2005-specification(amanded)-(21-12-2009).pdf

1263-MUM-2005-SPECIFICATION(AMENDED)-(21-12-2009).pdf

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Patent Number

238623

Indian Patent Application Number

1263/MUM/2005

PG Journal Number

8/2010

Publication Date

19-Feb-2010

Grant Date

15-Feb-2010

Date of Filing

07-Oct-2005

Name of Patentee

MALSHE VINOD CHINTAMANI

Applicant Address

1, Staff Quarters, UDCT Campus, Matunga, Mumbai-400 019

Inventors:

#	Inventor's Name	Inventor's Address
1	MALSHE VINOD CHINTAMANI	1, Staff Quarters, UDCT Campus, Matunga, Mumbai-400 019
2	DAMLE ADITI SHARAD	1, Staff Quarters, UDCT Campus, Matunga, Mumbai-400 019

PCT International Classification Number

B01D53/22

PCT International Application Number

N/A

PCT International Filing date

PCT Conventions:

#	PCT Application Number	Date of Convention	Priority Country
1			NA