WO2017018764A1 - Procédé de concentration de solution aqueuse contenant un soluté à haute concentration par procédé d'osmose inverse dans un état de différence de pression non-osmotique - Google Patents

Procédé de concentration de solution aqueuse contenant un soluté à haute concentration par procédé d'osmose inverse dans un état de différence de pression non-osmotique Download PDF

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WO2017018764A1
WO2017018764A1 PCT/KR2016/008104 KR2016008104W WO2017018764A1 WO 2017018764 A1 WO2017018764 A1 WO 2017018764A1 KR 2016008104 W KR2016008104 W KR 2016008104W WO 2017018764 A1 WO2017018764 A1 WO 2017018764A1
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solute
osmotic pressure
aqueous solution
chamber
water
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PCT/KR2016/008104
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English (en)
Korean (ko)
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장호남
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장호남
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Priority to EP16830797.3A priority Critical patent/EP3326977A4/fr
Priority to US15/744,945 priority patent/US10953367B2/en
Priority to JP2018523724A priority patent/JP2018520874A/ja
Priority to CN201680049525.1A priority patent/CN108137351A/zh
Priority claimed from KR1020160094090A external-priority patent/KR101865342B1/ko
Publication of WO2017018764A1 publication Critical patent/WO2017018764A1/fr
Priority to SA518390792A priority patent/SA518390792B1/ar

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis

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  • the present invention relates to a method of concentrating a solute-containing aqueous solution at high concentration, and more particularly, to a method of concentrating a solute-containing aqueous solution to be concentrated at a high concentration by removing water by a hydraulic-membrane process in the absence of an osmotic pressure difference.
  • RO Reverse osmosis
  • Table 1 compares the advantages and disadvantages of the forward osmosis (FO) regeneration method and the method of concentrating the solute-containing aqueous solution at a high concentration by the hydraulic-membrane process in the absence of an osmotic pressure difference.
  • RO has only 50% solvent recovery and most of all, it is difficult to operate at 343.070 bar of 3% -NaCl saturated solution (26.47%) to recover 100% solvent and solute.
  • FO has the advantage of operating at atmospheric pressure, but it is necessary to regenerate the draw solution and it is not easy to recover the solute when the solute in the feed crosses to the draw solution (Jung et al. Process Biochemistry (2015) 50 (4) 669-677 ).
  • the flux of the solvent (water) and the movement of the solutes (salt, VFA, ethanol) are as follows.
  • Jw is the water flux
  • Lp is the water permeation coefficient
  • ⁇ P is the hydraulic pressure difference between the feed chamber and the draw chamber
  • ⁇ is the osmotic pressure difference between the feed chamber and the draw chamber.
  • the Js is divided into one due to the difference in osmotic pressure and one due to the flux of the solute.
  • the solute When there is no Jw in Equation (2), the solute may move to the feed chamber by the draw chamber due to the osmotic pressure difference.
  • C means concentration
  • R means gas constant
  • T means temperature
  • Vsp is the volume of 1 mole of solvent when the solute concentration is 0
  • ⁇ is the activity coefficient of the solvent
  • X is the mole fraction of the solute.
  • the salt When 30 g / L of solute is dissolved in water, the salt has an osmotic pressure of 25.4 bar, albumin 0.01 bar and particles 1.2x10 -12 bar.
  • Reverse osmosis and forward osmosis have the advantage of saving energy by using membranes, but as the concentration progresses, the osmotic pressure in the feed chamber increases, making it impossible to concentrate the feed solution or increase the utilization of the feed solution (Loeb, S, Loeb-Sourirajan Membrane, How it Came About Synthetic Membranes, ACS Symposium Series, 153, 1, 1-9, 1981; Loeb, S., J. Membr. Sci, 1, 49, 1976).
  • the substances that humanity needs are in the form of solids, liquids, and gases in the ocean, land, and atmosphere, and exist as independent molecules or compounds.
  • the desired material can be obtained through catalysts, chemical reactions, bioreactions and the like.
  • the inventors have developed a method for concentrating a solute-containing aqueous solution using a non-osmotic pressure concentrator including a feed chamber composed of a forward osmosis and / or reverse osmosis membrane and a ⁇ -echolizer chamber to obtain the above materials (International Patent PCT / KR2014 / 000952).
  • the above technique uses a part of the concentrate as an induction solution.
  • the high osmotic pressure difference formed between the feed chamber and the ⁇ -echolizer chamber has to be overcome.
  • the above patent used a method of reducing the residence time of the ⁇ -echolizer solution in the ⁇ -echolizer chamber, but found a problem with the design of the ⁇ -echolizer and required a new method.
  • the present invention (a) concentrating the solute-containing aqueous solution using an osmotic pressure difference concentrator comprising a feed chamber and a ⁇ -echolizer chamber partitioned with a reverse osmosis membrane, one of the following processes Forming a ⁇ reduction condition between the feed chamber and the ⁇ -echolizer chamber using the above process: (i) (Feed) Input-split cascade process; (ii) (Feed) Output-split counter-current process; And (iii) applying the nano filtration membrane and (b) recovering the concentrated solute-containing aqueous solution using another osmotic pressure difference concentrator or reverse osmosis.
  • an osmotic pressure difference concentrator comprising a feed chamber and a ⁇ -echolizer chamber partitioned with a reverse osmosis membrane
  • 1 is a diagram illustrating a process of separating 970 g of water and 30 g of salt in a NaCl solution of 3% (w / w) in a zero / low osmotic pressure difference of the present invention
  • 1 and 2 indicate a normal reverse osmosis process
  • 3 Means an osmotic pressure difference concentrator.
  • FIG. 2 is a schematic diagram of three methods used to achieve the osmotic pressure / low osmotic pressure difference of the present invention
  • the osmotic pressure difference is zero and the feed chamber is concentrated, the feed chamber is concentrated and the ⁇ -Equalizer chamber is diluted so that osmotic pressure difference can occur.
  • B is the Feed Output-Split CC (counter-current) method.
  • both streams flow counter-current.
  • the starting concentration of the feed chamber is 6%
  • the final concentration of the ⁇ -Equalizer stream can be made 3%.
  • C indicates that the use of a membrane with a low solute reflection coefficient allows some of the solute in the feed stream to flow into the ⁇ -Equalizer stream to reduce the osmotic pressure difference.
  • the graph on the left shows the difference between the two chambers according to these three methods. Osmotic pressure difference is shown.
  • (a) is a high pressure feed chamber (A) and an atmospheric pressure draw chamber ( It is an explanatory drawing of a BPS system including B), and
  • (B) is a specific design drawing of A and B.
  • FIG. 4 is a system diagram that can separate 3% NaCl solution into water and 26.47% saturated solution (or salt) using an input-split cascade system.
  • the water is discharged to the outside of the various types of solute-containing aqueous solution to be concentrated using a reverse osmosis separator, and the concentrated aqueous solution includes a feed chamber and a draw chamber partitioned by a reverse osmosis membrane or an forward osmosis membrane.
  • the osmotic pressure difference between the feed chamber and the draw chamber is a low osmotic pressure / no osmotic pressure state It was confirmed that it can be maintained as.
  • the question of whether the feed should be limited to the solute-containing solution after recovering the water by reverse osmosis in a non-osmotic pressure difference concentrator confirms that the total energy consumption is reduced while reducing the amount of water drawn from the solute-containing solution (3%) by reverse osmosis, and pure 3% brine (sea water), which has not undergone reverse osmosis-pure manufacturing, Even when added, it was confirmed that the solvent and the solute can be separated with high efficiency.
  • the present invention in one aspect, (a) the solute-containing aqueous solution is concentrated using an osmotic pressure concentrator comprising a feed chamber and a ⁇ -echolizer chamber partitioned with a reverse osmosis membrane, wherein at least one of Forming a ⁇ reduction condition between the feed chamber and the ⁇ -echolizer chamber using the process: (i) (Feed) Input-split cascade process; (ii) (Feed) Output-split counter-current process; And (iii) applying a nano filtration membrane; And (b) recovering the concentrated solute-containing aqueous solution using another osmotic pressure difference concentrator or reverse osmosis pressure.
  • an osmotic pressure concentrator comprising a feed chamber and a ⁇ -echolizer chamber partitioned with a reverse osmosis membrane, wherein at least one of Forming a ⁇ reduction condition between the feed chamber and the ⁇ -echolizer chamber using the process: (i)
  • step (c) another non-intrusive pressure difference concentrator of step (b) further comprises the step of maximizing the recovery of the solute using one or more of the processes (i) to (iii). can do.
  • the step (a) may be characterized in that it further comprises the step of concentrating the solute-containing aqueous solution to be concentrated before using the reverse osmosis.
  • the step (b) of concentrating the solute-containing aqueous solution using another osmotic pressure difference concentrator transfers the concentrated aqueous solution to the feed chamber of the osmotic pressure difference concentrator, and is transferred to the feed chamber. Injecting a solution having the same osmotic pressure as the concentrated aqueous solution into the draw chamber to form an osmotic pressure state between the feed chamber and the draw chamber; And (ii) a pressure of up to 0 to 5 atm for forward osmosis (FO) and 10 to 200 atm for reverse osmosis is applied to the feed chamber at zero osmotic pressure, and the water in the concentrated aqueous solution is drawn. And further concentrating the concentrated aqueous solution by transferring to the chamber.
  • a pressure of up to 0 to 5 atm for forward osmosis (FO) and 10 to 200 atm for reverse osmosis is applied to the feed chamber at zero osmotic pressure, and the water in the concentrated a
  • the osmotic pressure difference between the feed stream supplied to the feed chamber and the ⁇ -echoizer supplied to the ⁇ -echolizer chamber is increased (i) an input-split cascade process; (ii) an output-split counter-current process; Or (iii) using the process of applying the nano filtration membrane to reduce the difference.
  • the terms “(feed) input-split cascade process” and “input-split cascade process” refer to half of the feed solution fed to the osmotic pressure concentrator and half to the feed chamber, and half to the ⁇ -echoiser chamber. After forming the osmotic pressure difference, the aqueous solution of the feed chamber is concentrated at low pressure, and the concentrated solute-containing aqueous solution is transferred to another osmotic pressure concentrator.
  • ⁇ reduction condition means a condition in which there is no osmotic pressure difference or a very small value between the feed chamber and the ⁇ -echolizer chamber. That is, the ⁇ reduction condition of the present invention means a case where ⁇ is 0 or 1 to 100 bar or less.
  • (feed) output-split counter-current process” or “output-split counter-current process” of the present invention is characterized by sending a portion of the ⁇ -echolizer stream to the feed stream in a concentrated state in an osmotic pressure concentrator. You can do
  • ⁇ (Pai) -echolizer chamber of the present invention is used in the same sense as the draw chamber, and the dilution of the filter liquid (water) in the feed stream is the same, but the maneuverability in the orthostatic method is concentrated in the draw chamber. Compared to the induction solution, the difference here is the hydraulic pressure ( ⁇ P).
  • ⁇ P hydraulic pressure
  • step (a) may apply steps (i) to (iii), respectively, and (i) and (ii), (i) and (iii), (ii) and (iii) or (i) )) To (iii) may be applied to form the ⁇ reduction conditions.
  • 3% brine is completely converted into crystalline form (solid content) by reverse osmosis in 3% NaCl solution in 26.47% saturated solution by input-split cascade process and output-split counter-current process.
  • the process of concentration was simulated and consulted with a crystallization expert to get advice.
  • the input-split cascade process (Figure 2A) is divided into feed stream and ⁇ (osmotic pressure) -echolizer stream for each concentration section, solute remains in the feed chamber and only solvent, water, is moved to the ⁇ -echoiser to increase the solution concentration in the feed chamber.
  • ⁇ -echolizer decreases.
  • When recovering the salt in the present invention may be characterized by applying a method using thermal energy or electrical energy well known to those skilled in the art in a saturated solution, or by applying a feed input-split cascade process and a feed output-split counter-current process It is not limited to this.
  • the present invention may be characterized by using a nanofiltration membrane.
  • the step (iii) of the step (a) is selected from the beginning when applied to the process (i), the initial selectivity in consideration of the degree of concentrated water recovery and osmotic pressure difference when applied to the process (ii)
  • the higher the late membrane, the greater the osmotic pressure difference may be characterized in that the osmotic pressure difference can be reduced by selecting a membrane with low selectivity, but is not limited thereto.
  • the reverse osmosis method may be used when producing pure water, and the RO process may be used as a system when producing water.
  • the saturated solution concentrated by the method of the present invention can produce power using PRO (pressure retarded osmosis) method using river water or seawater.
  • the osmotic pressure difference concentrator according to the present invention may be composed of a plurality. That is, the feed chamber and the ⁇ -echolizer chamber constituting the osmotic pressure difference concentrator are characterized in that it is composed of a multi-stage.
  • the reverse osmosis membrane or the forward osmosis membrane partitioning the feed chamber and the draw chamber of the osmotic pressure difference concentrator may be used without particular limitation as long as it does not pass the solute and mainly passes the solvent.
  • the solute means a liquid or solid substance dissolved in water as a solvent.
  • the solute-containing aqueous solution to be concentrated may include sea water, brackish water, cell metabolites, reaction solutions, and the like, and cell metabolites may be cultured cells of animal cells, plant cells, or microorganisms.
  • the concept includes a primary product, a secondary product, an in vitro secreted protein, a biotransformation, and the like, but may be a suitable process when the molecular weight is small and the osmotic pressure is high.
  • reaction solution examples include a reaction solution through a chemical reaction and a reaction solution through an enzyme reaction.
  • the primary products of the microorganisms include organic acids (acetic acid, propionic acid, butyric acid, lactic acid, citric acid, lactic acid, succinic acid, etc.), alcohols (ethanol, butanol, etc.), nucleic acids, amino acids (lysine, tryptophan, etc.), vitamins, polysaccharides, and the like. It may be illustrated, but is not limited thereto.
  • the secondary products of the microorganisms include antibiotics (such as lung nicillin), enzyme inhibitors, physiologically active substances (taxols, etc.), and the in vitro secreted proteins of the microorganisms include enzymes such as amylase and cellulase, insulin, interferon, and single group antibodies.
  • antibiotics such as lung nicillin
  • enzyme inhibitors such as a carboxyl-containing carboxyl-containing carboxyls, etc.
  • the in vitro secreted proteins of the microorganisms include enzymes such as amylase and cellulase, insulin, interferon, and single group antibodies.
  • the biotransformation of the microorganism is a substance produced by using a microorganism or an enzyme, and examples thereof may include steroids, but are not limited thereto.
  • the concentration of ethanol can be concentrated in a reverse osmosis concentrator (RO-1) is about 20%, theoretically 20 ⁇ by the osmotic pressure difference method It is known to be able to concentrate up to 100%.
  • RO-1 reverse osmosis concentrator
  • the saturation degree is about 50 to 60 wt%, so it is theoretically possible to concentrate 100%, and the high solute rejection rate is also 100% concentrated in the absence of osmotic pressure difference.
  • the solute low selectivity membrane is a membrane having a selectivity lower than 1 and higher than 0, which generally corresponds to a nanofiltration membrane, but is not limited thereto.
  • the target material when the target material is a solid, it is easy to crystallize according to temperature and pH, and is suitable for a material having high viscosity at high concentration.
  • alcohol for fuel may be a good application but is not limited to this.
  • the pH of the aqueous solution is 2-13
  • the temperature is the temperature at which water maintains the liquid (usually 0 to 100 °C, preferably 15 to 50 °C, more preferably 20 to 40 °C) or more Or can be For example, mixtures with other solutes / solvents may deviate from the above temperatures.
  • a concentrated aqueous solution transferred to the feed chamber a solution that can be easily separated after use, and the like may be used. It is preferable to use an aqueous solution of the same composition as the concentrated aqueous solution transferred to the feed chamber.
  • the concentration using the osmotic pressure difference concentrator may be performed in a batch or continuous manner to maximize the effect.
  • the batch may be performed when there is no flow with both chambers and the external system, and the continuous may be performed when there is a flow with the external system.
  • the feed chamber and the ⁇ -equalizer chamber is characterized in that it is composed of a multi-stage.
  • the method of recovering the solute and the water from the aqueous solution further concentrated in the osmotic pressure difference concentrator is independently a commonly known multistage evaporation method, dialysis evaporation, pyrolysis method, sulfuric acid method, calcium method and input-split. cascade may be used, but is not limited thereto.
  • the concentration method further comprises the step of (d) maximizing the recovery of either solute or water using any one of the steps (i) to (iii) of step (c). It can be characterized.
  • the pressure-added forward osmosis (PRO) power generation, resource utilization and rare earth recovery process may be further included to increase the added value of the process.
  • it may further comprise a step of optimizing the material balance and the energy balance.
  • the present invention also relates to a method for separating a solvent and a solute from a solute-containing solution using the above concentration method.
  • the solute is a salt
  • the solvent may be characterized in that the water.
  • Table 4 calculates the osmotic pressure of 3% NaCl, the description of each column of the table is as follows.
  • # 1: w / w% is the weight ratio of water and salt.
  • 3% brine consists of 970kg water and 30kg salt
  • # 5 The amount of energy required to produce one ton of water with an unchanged percentage of raw water at each concentration.
  • volume 1 is the amount of water contained in each% solution based on 30 kg of salt.
  • a sample (NaCl aqueous solution) is put in the apparatus as shown in FIG.
  • the membrane used in this example is RE2521-TL (Woongjin Chemical Co, Seoul, Korea; http: //www.csmfilter.com) Ltd, which is a thin-film composite type and the membrane is used in a negatively charged, polyamide, spiral-wound module.
  • RO membrane The permeability is 1.1m 3 / day and the effective area is 1.1m 2 . 99% rejection at 1,500mg / L salt solution, 1.0MPa, maximum pressure is 4.14MPa, maximum flow rate is 1.36m 3 / hr, minimum flow rate (concentrate) is 0.23m 3 / hr.
  • the maximum temperature is 45 ° C. and the pH is 3.0-10.0 and can withstand 2.0-11.0.
  • the 1.5 to 3% portion has a linear relationship where the plus is above the critical pressure, but at subsequent concentrations it is proportional to ( ⁇ P) ⁇ (C) ⁇ where ⁇ is 0 to 1 and ⁇ is -1 to 0 are displayed.
  • concentration the lower the flux and the higher the pressure.
  • the maximum pressure was 40 bar.
  • Example 3 100% Separation of Solute / Solvent Based on Feed Input-Split Cascade Process
  • the process of the present invention is capable of producing an input stream of 3%, a water production system at the bottom, a saturated concentrated solution at the top or a salt thereof.
  • the 3% solution produces 500 L of pure water and enters the 6% chamber with 6%, 470 L water (total 500 kg solution).
  • the input-split method is used to separate 9% concentrate and 3% solution, 6% of which is a 9% chamber at the top, 3% of which produces 235 kg of raw water in the RO-2 unit, and the remaining 235 kg enters the chamber as Recycle. . 9 ⁇ 12 ⁇ 15 ⁇ 18 ⁇ 21 ⁇ 24 ⁇ 26.47% (sat.) And the diluted stream was recovered to 26.47% ⁇ 21% ⁇ 18 ⁇ 15 ⁇ 12 ⁇ 9 ⁇ 6 ⁇ 3 ⁇ 0 (pure) do.
  • Flux movement and energy consumption by solute concentration are 371 kg of total water moved through the membrane in feed input-split cascade.
  • a total pressure of 0.309 Kwh is required at an average pressure difference of 30 bar, and two recycles are required to remove 30 kg of salt.
  • the total energy required is 0.618kwh.
  • 9 steps of mixing and demixing occur from 3% to 26.47%. However, a considerable amount of water can be recovered in steps 1 and 2, which can be considered if not all of the water is recovered.
  • the feed input is 6%, 470L, 30g in the osmotic pressure difference condensation process.
  • the water moves to the chamber by ⁇ -evaporator.
  • the R on the right shows how much salt total flows from the feed chamber end stream to the product (draw) chamber.
  • the concentration is 26.47% at the feed chamber end.
  • the ⁇ -echoarizer is 3.38% and the amount of water recovered is 428.33 kg. This is the amount when the product is a saturated solution.
  • the energy consumption varies greatly depending on the size of the sample entering the target RO apparatus. For example, if you remove 1 ton (100 liters of water and 30 kg of salt) from 100 tons of raw water, the minimum energy will be very small.
  • the energy consumption was only about 10% when a large separator was used at the feed input, but in fact energy consumption is highly related to the recovery rate.
  • the inputs of F250, F485, and F500 RO-1 are 3% brine and the concentration of the output according to the recovery degree of RO-1 entering the recycle stream.
  • the concentration was low, and as in the F500, the recovery of 500L in RO-1 was confirmed to be 6%.
  • the first row is the energy required to recover pure water from 3% brine in the RO-1 unit, and the RO-2 is the energy consumed in the recycle unit.
  • the last one is the desalination process from F250 of Example 2 (3.5S, 3.5Ws). Is the energy required.
  • RO-2 The calculation of RO-2 was performed as follows.
  • RO-2 input (top water) The difference in the output of the bottom water is multiplied by the amount of recycled water divided by 36 to get kwh.
  • the energy difference was obtained by multiplying the pressure difference between feed-output (26.47%) and sub-water input (23.57%) by 41.67.
  • the energy difference between the first and last energy was calculated from the recycling system, the arithmetic mean was calculated, and the total recycled water was multiplied to obtain a simple recycle energy.
  • the cost of water production of RO-2 is the ⁇ process cost, plus 3% of the water production cost from the solution entering the raw water tank.
  • the cumulative total of the three processes shows a low F250 of 1.236 but F485 or The F500 has significantly higher total energy requirements of 1.528 and 1.540, which is not significantly different from “Input-split Cascade” or “Output-split CC.” These values are based on the use of one ton of solute solution.
  • the recovery of salt at low pressure and 100% recovery of water can be significant.
  • Low selectivity membranes are applied to the input-split cascade and output-split CC to significantly improve the membrane flux and to save energy for the recycling process.
  • the current use of the RO process is one There needs 1kwh / m 3 to overcome the minimum osmotic pressure difference in the production of water per ton to overcome the osmotic pressure actually is 2kwh is consumed 2kwh, yet other processes in the osmotic process, the RO process, the total 4kwh Is known to be consumed.
  • the cost of electric energy is $ 1 per ton of water, it is very important to reduce it to a little since 40% of the cost of water is assumed to be $ 0.1 / kwh.
  • the difference in concentration is 1%
  • one method may be to input-split at first and then switch to output-split later.
  • Example 6 F500, F485, and F250 first examined 500L, 485L, and 250L recovery through RO in 970L water of 3% raw water. Then, let's consider recirculation of RO-1, which is the extreme condition, all zero.
  • Feed input 3%, 970 L + 30 kg salt and the recycle stream of the ⁇ -echolizer chamber will be 1.52% with 970 L + 15 kg salt water.
  • the osmotic pressure of 3% is 23.743 bar and the osmotic pressure of 1.52% is 11.746 bar.
  • the difference between the two osmotic pressure is 11.997 bar, the average is 17.744 bar.
  • the pressure difference at the input is 11.997 bar and the pressure difference at the input outlet (26.47%) / pi-Equalizer start point is 55.148 bar.
  • High pressure in the middle process is not a problem because there are many solutions such as low ⁇ membrane or input-split cascade.
  • RO-1 uses only an average of 3% and 4%, later using both an average of 4% and 2.04% and pressure difference in recycle energy.
  • the input of the ⁇ -equalizer chamber be 15S, 41.67W (1/2 of the concentrated water component) and 23.57% (Example 6).
  • Ethanol for fuel is currently used in 99.5% or 99.6% purity. There is a thermal method (gas generates steam, electricity is used). According to the Renewable Fuels Association (March 06, 2016) in the United States, the minimum energy is 23,424 BTU / gal from Iowa WDG. If you change this to kwh / kg-fuel ethanol, you get 2.27kwh / kg-ethanol. Here, the concentration of up to 99.5% by applying an osmotic pressure difference RO technology will be considered.
  • Table 10 calculated the osmotic pressure of the alcohol by Lewis equation (eq.-4). Initially it goes up to 28 bar at 5% or 6010 bar at 99.50%. Unlike high pressures, high pressures have very low volume, which results in very low energy content. Like 3% -NaCl, most of the energy content is concentrated at low concentrations.
  • the energy required for concentration can be calculated.
  • the energy required for concentration up to 5% 99.5% is 0.08819 kwh / kg, 10% ⁇ 99.5% is 0.0373kwh / kg and 7% ⁇ 99.5% is 0.04787kwh / kg.
  • the osmotic pressure difference technology can make the pressure level that we can handle (e.g. below 100 bar).
  • the membrane is used, the azeotrope phenomenon between water and ethanol is also achieved. It can be said that it can be solved.
  • the global desalination market is 60 million / d, according to 2016 (google image: desalination market accessed on 07-24-2016).
  • An economic evaluation was conducted on the 65,000 ton / d seawater desalination plant in Gijang-gun, Busan, Korea. Economics compared the price of water at $ 1 per tonne based on the current international price of each element.
  • the method of concentrating an aqueous solution by hydraulic pressure in a non-osmotic pressure difference state consumes less energy and can be concentrated until the maximum saturated aqueous solution concentration or the concentration of the solute is 100% without using an extraction solvent. There is an advantage that does not need to use a separate osmotic induction solution.

Abstract

La présente invention concerne un procédé pour concentrer une solution aqueuse à basse pression dans un état de différence de pression non-osmotique et, plus spécifiquement, un procédé pour concentrer une solution aqueuse contenant un soluté afin d'être concentrée à basse pression dans un état de pression non-osmotique. Lorsque le procédé de la présente invention est utilisé, la consommation d'énergie est réduite, et la solution aqueuse peut être concentrée, sans utiliser de solution d'extraction, jusqu'à ce que la solution aqueuse saturée du soluté maximal soit préparée ou la concentration du soluté soit de 100 %. De plus, le procédé présente l'avantage de ne pas nécessiter l'utilisation d'une solution d'induction osmotique distincte.
PCT/KR2016/008104 2015-07-24 2016-07-25 Procédé de concentration de solution aqueuse contenant un soluté à haute concentration par procédé d'osmose inverse dans un état de différence de pression non-osmotique WO2017018764A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
EP16830797.3A EP3326977A4 (fr) 2015-07-24 2016-07-25 Procédé de concentration de solution aqueuse contenant un soluté à haute concentration par procédé d'osmose inverse dans un état de différence de pression non-osmotique
US15/744,945 US10953367B2 (en) 2015-07-24 2016-07-25 Method of osmotic pressure free reverse osmosis for enriching solute-containing solution to high concentration
JP2018523724A JP2018520874A (ja) 2015-07-24 2016-07-25 溶質含有水溶液を高濃度に濃縮するための浸透圧を用いない逆浸透圧法
CN201680049525.1A CN108137351A (zh) 2015-07-24 2016-07-25 用于将含有溶质的溶液富集成高浓度的无渗透压反向渗透的方法
SA518390792A SA518390792B1 (ar) 2015-07-24 2018-01-23 طريقة تناضحية عكسية خالية من الضغط التناضحي لتعزيز محلول يحتوي على مادة مذابة إلى تركيز عالٍ

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