• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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    • 专利摘要:
    The present invention falls within the field of chemical and environmental technologies, and refers to a system and a method of high energy efficiency for the concentration of saline solutions (which can be generically referred to as brines) and/or recovery of the water contained therein. These brines can be generated in numerous industrial sectors, such as: desalination plants, plants associated with drilling for the extraction of gas and oil, power generation plants, leather tanning plants, food canning and dressing plants. olives, salted, oil mills, curing hams and sausages, as well as all those that treat high volumes of water (decalcification, demineralization, reverse osmosis, etc.). (Machine-translation by Google Translate, not legally binding)
    公开号:ES2779982A1
    申请号:ES201930141
    申请日:2019-02-20
    公开日:2020-08-21
    发明作者:Arenas Luis Francisco Vilches；Torralvo Fatima Arroyo；Pereira Constantino Fernandez；Galan Monica Rodriguez
    申请人:Universidad de Sevilla；
    IPC主号:
    专利说明:

    [0001] SYSTEM AND METHOD FOR THE CONCENTRATION OF SALINE SOLUTIONS
    [0003] OBJECT OF THE INVENTION
    [0005] The present invention is included in the field of chemical and environmental technologies, and refers to a system and a method of high energy efficiency for the concentration of saline solutions (which can be generically referred to as brines) and / or recovery of the water contained therein. These brines can be generated in numerous industrial sectors, such as: desalination plants, plants associated with drilling for the extraction of gas and oil, power generation plants, leather tanning plants, food canning and dressing plants. olives, salted fish, oil mills, ham and sausage curing, as well as all those that treat high volumes of water (decalcification, demineralization, reverse osmosis, etc.).
    [0007] BACKGROUND OF THE INVENTION
    [0009] Freshwater scarcity is one of today's most important global challenges and represents a threat to the growth, security and balance of nations and ecosystems. The supply of drinking water in many territories is becoming even more complicated with climate change. One type of aqueous stream that is produced in a wide variety of processes are streams with high salinity (generically referred to as brines), which, in most cases, cannot be directly discharged into the receiving environment. For the management of these streams, it is not always easy to find a competitive management route, as there are different alternatives, such as deep injection, evaporation ponds, obtaining valuable products and treatment of the brine through a zero discharge system ( ZLD, English terms for "Zero Liquid Discharge"). Of all the previous options, the latter stands out for its versatility and for being the most respectful with the environment, since it practically does not produce any discharge. This technology generates on the one hand, a high-quality water effluent that can be reused in the production process, and on the other, a crystallized saline product is obtained that can be recovered.
    [0010] In recent years, there has been an evolution in ZLD systems, from those based on thermal processes to membrane-based processes, with reverse osmosis (RO) being one of the technologies that has been incorporated into ZLD systems to improve energy efficiency and reduce costs. However, although RO is more efficient than thermal evaporation, it can only be applied to feed waters with a limited salinity range. Consequently, other emerging brine concentration technologies to treat higher salinity streams, such as electrodialysis (ED), direct osmosis (FO), membrane distillation (MD), and osmotically assisted reverse osmosis (OIAO) are being developed. incorporating as alternative technologies in ZLD systems to concentrate the brines.
    [0012] Electrodialysis applies an electric potential as a driving force to remove dissolved ions through ion exchange membranes. In contrast to RO membranes that reject all ions, ion exchange membranes selectively reject cations or anions. In a variant of ED, reversible electrodialysis (EDR), the polarity of the electrodes is frequently reversed to minimize fouling, so fewer pretreatments are required than with RO. The problems of ED / EDR processes in brine treatment systems are due to high energy consumption. In addition, it is necessary to use a multi-stage configuration, which increases the capital cost.
    [0014] In membrane distillation, the feed water is heated and the difference in temperature between the hot feed water (typically 60-90 ° C) and the cooler permeate side water creates a difference in fugacities of the driving steam. the flow of water vapor. In the treatment of brines, MD can be of interest due to its ability to treat high salinity feed waters that cannot be treated by RO. Additionally, MD can harness low-exergy thermal energy. When this low-exergy energy is available, MD techniques can reduce the carbon footprint relative to electricity-powered technologies. In addition, the MD is modular, operates at low pressure and low temperature, and has a low propensity for fouling. However, when there are volatile contaminants in the feed water, MD membranes do not retain volatile compounds, with consequent deterioration of product water quality and reduced process efficiency.
    [0016] Direct Osmosis uses a difference in chemical potentials (osmotic pressures) as a driving force to permeate water through a semi-permeable membrane.
    [0017] In direct osmosis, water flows from the feed solution into a concentrated extraction solution (entrainment solution) of higher osmotic pressure. The development of thermolytic solutions such as ammonium-carbon dioxide (NH3 / CO2) solutions has allowed the incorporation of FO into ZLD systems. Because the NH3 / CO2 extraction solution decomposes at a moderate temperature (approximately 60 ° C and atmospheric pressure), its regeneration can be done with low-exergy energies, residual energies from processes, and geothermal energy. Another advantage of FO is that it operates at low pressure, resulting in layers of fouling on the membranes that are less compact and easier to clean than fouling on RO membranes. Consequently, fouling of FO membranes is more reversible than those of the RO process. This fact reduces the operating cost for fouling control, and extends the applicability of FO in ZLD systems to streams with high fouling potential.
    [0019] Osmotically assisted reverse osmosis is a variant of traditional RO that allows water to be recovered from high salinity solutions at room temperature. The feed is introduced into the high pressure chamber (of the order of 60 bar) of an RO module (generally of the spiral or flat type). On the opposite side (low pressure chamber), a current with a salinity lower than the feed, but not negligible, flows countercurrently, as occurs with the permeate current in conventional RO. This current can be called a sweeping solution in Spanish. A hydraulic pressure difference is established between the feed and sweep solutions which, when it is greater than the osmotic pressure difference between the two faces of the active membrane layer, causes a flow of water from the feed to the swept. Loss of water from the feed stream causes dilution of the sweep stream. Depending on the solute concentration with which the diluted scanning solution comes out, it can be established that:
    [0020] - if it is less than a certain value (e.g .: <10 g / L NaCl) it can be sent directly to a conventional RO unit operating at moderate pressure, or,
    [0021] - if it is greater, it is treated as the new supply of a second unit for which another pressurization is necessary in a second pumping unit.
    [0023] Therefore, the entire process consists of a series of successive stages of osmotically assisted RO with a last stage of conventional RO. The number of pumping equipment (plus energy recovery units) and membrane units depends, among others, on the degree of concentration to be achieved and the pressures applied. The process of Osmotically assisted osmosis allows the membrane units to operate with hydraulic pressures of the same order as those used in conventional desalination processes (50-70 bar), which implies high energy efficiency. The disadvantage of this technology is the investment cost of the N pump units, energy / pressure exchangers and membrane modules.
    [0025] From the point of view of the technical-economic viability of the process, the critical variables of the OIAO process are the area of the membranes and the number of OIAO modules required for each type of brine. In general, the OIAO process involves high capital investment costs due to the use of various membrane modules, high pressure pumps and energy / pressure exchangers, so an optimized OIAO process should aim to achieve a small number of stages (eg: between 2 and 3 modules). Additionally, while membrane and module cleanings and replacements contribute to operating costs, the dominant factor in operating costs is linked to energy consumption. In this process, pretreatments are essential to reduce membrane fouling, especially in the case of high-salinity brines.
    [0027] In the line of OIAO processes, in the bibliography there are patents (US 9206061B1; WO 2016 / 189438A1; US 2016 / O339390A1; WO 2017 / 078644A2); and technical articles (Desalination 421, 2017, 3-11.) in which the treatment of saline aqueous streams is described, using multiple reverse osmosis (RO) units arranged in series with decreasing saline concentrations and at least one reverse osmosis unit in a final stage, in which a part of the concentrate is recycled back to the permeate or exit side of that same unit to provide a mixed permeate. The mixed permeate is subsequently passed to the permeate side of the previous reverse osmosis unit. This process is repeated in each of the previous stages. This increases the salt content of the liquid on the permeate side of each stage, thus reducing the differential concentration of the reverse osmosis membranes.
    [0029] The system and method for the concentration of aqueous saline solutions with water recovery of the present invention, solves all the above drawbacks.
    [0030] DESCRIPTION OF THE INVENTION
    [0032] A first object of the present invention refers to a system for the concentration of aqueous solutions with water recovery that allows water to be recovered from said saline solutions, using at least one reverse osmosis module (OIM), by means of which it is concentrated and recovers water, by filtering and sequential transfer of a certain amount of water between a series of reservoirs containing osmotic solutions of adequate concentrations. The proposed invention makes it possible to overcome the maximum salt concentration limit imposed on the supply of a conventional reverse osmosis (RO) system for concentration of brines, using an economical and energy efficient system.
    [0034] The system for the concentration of aqueous solutions with water recovery comprises:
    [0035] • at least one reverse osmosis module comprising a concentrate side, a permeate side and a plurality of membranes;
    [0036] • at least one first tank I containing a first osmotic solution, where the first tank I is configured to concentrate the first osmotic solution from an initial concentration Cii to a final concentration Cif, greater than the initial concentration Cii, due to the passage of said first osmotic solution on the concentrate side of the at least one reverse osmosis module;
    [0037] • at least one second tank I-1 containing a second osmotic solution, where the second tank I-1 is configured to dilute the second osmotic solution from an initial concentration Ci-1i to a first final concentration Ci-1f, lower than the initial concentration Ci-1i, due to the passage of said second osmotic solution through the permeate side of the at least one reverse osmosis module;
    [0038] where the at least one reverse osmosis module is configured to carry out the permeation of a mass difference of water Me-Ms corresponding to the difference between an initial mass of water Me in the first tank I and a final mass of water Ms of the first deposit I due to the concentration of the first osmotic solution from the initial concentration Cii to the first final concentration Cif; where the at least second reservoir I-1 is also configured to concentrate the second osmotic solution from the first final concentration Ci-1f to a second final concentration Ci'1f ', greater than the first final concentration Ci-1f, due to the passage of said second osmotic solution through the concentrate side of the at least one reverse osmosis module, and
    [0039] where the system also includes:
    [0040] • at least one third reservoir I-2 containing a third osmotic solution, where the third reservoir I-2 is configured to dilute the third osmotic solution from an initial concentration C '"2i to a first final concentration C'" 2f, lower that the initial concentration C '"2i, due to the passage of said third osmotic solution through the permeate side of the at least one reverse osmosis module, and
    [0041] where the at least one reverse osmosis module is also configured to carry out the permeation of a difference in mass of water Me'-Ms 'corresponding to the difference between an initial mass of water Me' in the second tank I-1 and a final mass of water Ms' from the second reservoir I-1 due to the concentration of the second osmotic solution from the first final concentration Ci-1f to a second final concentration Ci-1f.
    [0043] The system comprises a control device configured to adjust to desired values the mass differences corresponding to the difference Me-Ms between the initial mass of water Me in the first tank I and the final mass of water Ms in the first tank I and to the difference Me'-Ms' between the initial mass of water Me 'in the second tank I-1 and the final mass of water Ms' of the second tank I-1.
    [0045] Optionally, the system for the concentration of aqueous solutions with water recovery further comprises:
    [0046] • at least one initial tank M containing a saline solution, where the initial tank M is configured to concentrate the saline solution from an initial concentration CMi to a final concentration CMf, greater than the initial concentration CMi, due to the passage of said saline solution on the concentrate side of the at least one reverse osmosis module, and to transfer to the first tank I the difference (MeM-MsM) between an initial mass MeM of the at least one initial deposit M and a final mass MsM of the at least one deposit initial M; where the first tank I is also configured to dilute the first osmotic solution from the initial concentration Cii to the first final concentration Cif, less than the initial concentration Cii, due to the passage of said first osmotic solution through the permeate side of the at least one reverse osmosis module. Preferably, the system for the concentration of aqueous solutions with water recovery further comprises a pump B configured to pressurize the first osmotic solution contained in the first tank I or the second tank I-1 as a function of the sequential transfer of water, or of the saline solution contained in the initial tank M up to a first hydraulic pressure (Pf) previously as it passes through the concentrate side of the at least one reverse osmosis module.
    [0048] Optionally, the at least one reverse osmosis module is also configured to send to the second tank, the difference in water mass Me-Ms corresponding to the difference between an initial mass of water Me in the first tank I and a final mass of water More than the first deposit I.
    [0050] Optionally, the at least one reverse osmosis module is also configured to send to the third tank the difference in mass of water Me'-Ms 'corresponding to the difference between an initial mass of water Me' in the second tank I-1 and a final mass of water Ms' of the second tank I-1.
    [0052] The control device is also configured to adjust the difference in mass MeM-MsM, between the initial mass MeM of the at least one initial deposit M and the final mass MsM of the at least one initial deposit M, to desired values.
    [0054] Optionally, the permeate side of the at least one reverse osmosis module is arranged in countercurrent or isocurrent with the concentrate side of the at least one reverse osmosis module.
    [0056] Optionally, the system for the concentration of aqueous solutions with water recovery further comprises a membrane refining unit AM configured to filter the contents of the third tank.
    [0058] Optionally, the system comprises at least a fourth tank, so that the second tank becomes the third tank and the third tank becomes the fourth tank, and so on up to the number of tanks required depending on the concentration of the brine from which you want to recover the water and the desired water concentration.
    [0060] In order to provide an understanding of the embodiment of the invention, certain details are described which would be clear to a person skilled in the art. Therefore, the components that detail the invention are specified in a general way. By Therefore, the system for the concentration of aqueous solutions with water recovery optionally further comprises:
    [0061] • a set of pipes for the main lines, recirculations and purges, as well as valves;
    [0062] • a set of instruments, among which conductometers, level meters and flow meters can be found, not being limited to them;
    [0063] • a set of separating elements configured to compartmentalize and separate the inlet and outlet streams of the tanks, thereby improving the effectiveness and efficiency of the process;
    [0064] where the control device controls a flow rate and a pressure of the pumps and the set of valves and the set of instruments to operate the plurality of membranes and the at least one reverse osmosis module.
    [0066] A second object of the invention is a process for the concentration of aqueous saline solutions with water recovery carried out in the previous system, where the process comprises the following stages:
    [0067] • at least one first stage where the concentration of a first osmotic solution is carried out in the at least one first reservoir I from an initial concentration Cii to a final concentration Cif, greater than the initial concentration Cii, due to the passage of said first osmotic solution on the concentrate side of the at least one reverse osmosis module;
    [0068] • at least one second stage where the dilution of a second osmotic solution is carried out in the at least one second reservoir I-1 from an initial concentration Ci-1i to a first final concentration Ci-1f, lower than the initial concentration Ci -1i, due to the passage of said second osmotic solution through the permeate side of the at least one reverse osmosis module;
    [0069] • at least a third stage where the permeation of a difference in the mass of water Me-Ms is carried out in the at least one module of reverse osmosis, the difference in the mass of water Me-Ms corresponding to the difference between an initial mass of water Me in the first tank I and a final mass of water Ms from the first tank I as a consequence of the at least one first stage;
    [0070] • at least a fourth stage where the concentration of the second osmotic solution is carried out in the at least one second reservoir from the first final concentration Ci-1f to a second final concentration Ci-1f, greater than the first final concentration Ci- 1f, due to the passage of bliss second osmotic solution on the concentrate side of the at least one reverse osmosis module;
    [0071] • at least a fifth stage where the dilution of a third osmotic solution is carried out in at least a third reservoir I-2 from an initial concentration Ci-2i to a first final concentration Ci-2f, lower than the initial concentration Ci- 2i, due to the passage of said third osmotic solution through the permeate side of the at least one reverse osmosis module;
    [0072] • at least one sixth stage where the permeation of a difference in the mass of water Me'-Ms 'is carried out in the at least one module of reverse osmosis, the difference in mass Me'-Ms' corresponding to the difference between a mass initial water mass Me 'in the second tank I-1 and a final mass of water Ms' from the second tank I-1, as a consequence of the at least fourth stage,
    [0074] Optionally, the process for the concentration of aqueous solutions with recovery of water further comprises:
    [0075] • at least a seventh stage where the concentration of a saline solution M is carried out in the initial tank M, from an initial concentration CMi to a final concentration CMf, greater than the initial concentration CMi, due to the passage of said saline solution through the concentrate side of the at least one reverse osmosis module;
    [0076] • at least an eighth stage of transfer to the at least first deposit I of the difference (MeM-MsM) between an initial mass MeM of the at least one initial deposit M and a final mass MsM of the at least one initial deposit M; and
    [0077] • at least a ninth stage where the dilution of the first osmotic solution is carried out in the first tank I, from the initial concentration Cii to the first final concentration Cif, lower than the initial concentration Cii, due to the passage of said first solution osmotic on the permeate side of the at least one reverse osmosis module. Preferably, the method comprises at least a tenth stage where the pumping and pressurization is carried out in the pump of the first osmotic solution contained in the first tank I or the saline solution contained in the initial tank M up to a first hydraulic pressure ( Pf) prior to its passage through the concentrate side of the at least one reverse osmosis module.
    [0079] Optionally, the procedure comprises at least an eleventh stage where the at least one reverse osmosis module sends to the second tank, the difference of mass of water Me-Ms corresponding to the difference between the initial mass of water Me in the first tank I and the final mass of water Ms of the first tank I.
    [0081] Optionally, the procedure comprises at least a twelfth stage where the at least one reverse osmosis module sends to the third tank, the difference in mass of water Me'-Ms 'corresponding to the difference between the initial mass of water Me' in the second tank I-1 and the final mass of water Ms' from the second tank I-1.
    [0083] During the mass delivery from the first to the second tank or from the second to the third tank respectively and so on, the gradient of osmotic solute concentrations between the feed solution and the scanning solution must be maintained so that the pressure differences between the feed and sweep solutions (-n > - -ns = An) are less than the differences in hydraulic pressures (P f - P s = A P) applied to these currents in the membrane unit, which will produce a net mass flow (J OISOW ) from the first tank I to the second tank I-1, and according to the following expression:
    [0085] JOISO w = A [ A P-ct A ^ j = A [(P f -P s ) - a ( ^ (C fm ) - ^ (C sm )) j
    [0087] where, ^ (C fm ) and ^ (C sm ) are the osmotic pressures at the solute concentrations in the active layer of the membrane (feed, C fm and sweep, C sm ), respectively; A is the coefficient of water permeability in the membranes, in m2 s / kg; ya: the reflection coefficient (a <1). Note that if (P f - P s ) is greater than [ ^ (C fm ) - -n (C sm ) j, the water flow will be positive.
    [0089] Optionally, steps from the first to the sixth can be repeated as many times as necessary, depending on the concentration of brine to be treated.
    [0091] In this way, the process for the concentration of aqueous solutions with water recovery of the present invention allows the plurality of membranes of the at least one reverse osmosis module to be subjected to increasingly dilute osmotic solutions, which causes a certain washing effect on them, improving the behavior of the membranes.
    [0093] Optionally, the process also comprises a final filtering stage to refine the content of the third tank or last tank, depending on those necessary for the concentration or recovery of water objectives.
    [0094] DESCRIPTION OF THE DRAWINGS
    [0096] To complement the description that is being made and in order to help a better understanding of the characteristics of the invention, according to a preferred example of a practical embodiment thereof, a set of drawings is attached as an integral part of said description. where, for illustrative and non-limiting purposes, the following has been represented:
    [0098] Figure 1.- Shows a scheme of the system for the concentration of aqueous solutions with water recovery of the present invention.
    [0100] Figure 2.- Shows a scheme of the system and method for the concentration of aqueous solutions with water recovery of the present invention, where the first four stages of the method are carried out to later carry out the fifth and sixth stages.
    [0102] Figure 3.- Shows a scheme of the system and method for the concentration of aqueous solutions with water recovery of the present invention where the seventh and eighth stages of the method are carried out.
    [0104] Figure 4.- Shows a scheme of the system and method for the concentration of aqueous solutions with water recovery of the present invention where the final stage of the method is carried out.
    [0106] Figure 5.- Shows a method scheme for the concentration of aqueous solutions with water recovery of the present invention applied to an example to concentrate brines and recover water from them, applied to a ZLD system of wastewater by means of hybrid membrane systems .
    [0108] PREFERRED EMBODIMENT OF THE INVENTION
    [0110] An example of embodiment of the invention is presented in Fig. 5, which shows a scheme of the method for concentrating brines with water recovery, applicable to the recovery of water from the stripping solution used in an osmosis process direct (FO). The example contemplates a hybrid membrane process, which has been called FO + OISO, applied to a zero discharge system for wastewater (ZLD) based on reverse osmosis technologies. The application of reverse osmosis (RO) in ZLD systems is conditioned by two inherent limitations: fouling and fouling of the membranes and the higher level of salinity that can be treated. The fouling of the membranes reduces the water permeability and the life of the RO membranes. This problem is particularly significant in ZLD systems. For this reason, in ZLD systems with RO, it is necessary to pretreat the feed water through processes such as: chemical softening, pH adjustment and ion exchange or a low pressure membrane process, such as ultrafiltration (UF). and the RO process, the first stage of the FO + OISO process consists of the concentration of the rejection of the RO operation (whose typical composition of major ions is presented in Table 1), from a concentration S1 (for example, 32 g / l of Total Dissolved Solids, STD) to S2 (for example, 175 g / l of STD) in an FO module, using as a stripping solution a solution of NaCl that is diluted from a concentration Ce (for example 200 g / l ) down to a lower Cs concentration (eg 175 g / l) with fluxes of water through FO membranes typically ranging between 5 and 15 kg / m2h. In general, the range of Ce-Cs (200-175) g / l concentrations will be defined by the desired concentration factor. The diluted carryover solution is stored in a (transit) tank. Once a mass of Me kilograms of the diluted entrainment solution has been generated, it is unloaded and treated in batches in the OISO system. Therefore, this dilute entrainment solution (of concentration Cs) constitutes the saline solution described in the detailed description section of the invention (Me), which returns concentrated to a lung tank (returns a mass Ms, less than Me) with concentration Ce (greater than Cs, after Ms-Me kilograms of water have been transferred in the OISO unit).
    [0112] As already mentioned, the values of Ce and Cs can be chosen, knowing that the selected figure will affect both the number of necessary stages and the membrane area that will be required to carry out the OISO operation. It must be fulfilled that Ce / Cs = Ms / Me; so the greater the difference between Ce and Cs, the Ms-Me will also be greater. In the example described, in the corresponding time unit, for every 11.4 kg of dilute entrainment solution (Me of concentration Cs = 175 g / l), 10.0 kg of concentrated entrainment solution (Ms concentration Ce = 200 g / l). Therefore, in the OISO unit it will be necessary to transfer Me - Ms = 1.4 kg of water.
    [0115] Therefore, the first phase of the OISO process consists of the regeneration of said solution from Cs to Ce.
    [0117] The buffer tank allows the FO operation to be carried out continuously while the OISO operation is carried out in batches. In the operating cycle of the FO + OISO process, the recovery time of the 1.4 kg ("Me-Ms") in the OISO unit depends on the water flow in the OISO unit (JOISOW, of the order of 1-10 kg / m2 h, and its membrane area, AOISO in m2).
    [0119] If the process is to be carried out continuously, the time it takes to recover the 1.4 kg of water in the OISO system must coincide with the time in which said 1.4 kg of water is transferred into the FO unit from the rejection of the RO (S1 in Fig. 5) to the entrainment solution, which will depend on the flux per unit area in the FO unit (JFOW in kg / m2 h and the membrane area of the FO unit AFo , in m2). By this it is meant that both FO and OISO systems could be coupled in one continuous operation.
    [0120] In the second phase of OISO in the application example, a series of successive stages are carried out in order to pass sequentially the 1.4 kg of water ("Me-Ms") from tank M-1 to tank 1 In all stages, in the OISO unit, the osmotic solute concentration gradient between the feed solution and the scanning solution provides osmotic pressure differences between both solutions (An) that will be lower than the hydraulic pressure differences ( pe: Pf - Ps = AP = 50 bar) applied to these currents in the OISO unit With the data chosen for this application example, the number of stages M-1 is equal to 5 (as shown in Table 2); but this number can be increased or decreased by varying the hydraulic pressures and the difference in osmotic pressures that are controlled by the osmotic solute concentration and flow rates at each stage.
    [0122] Table 2: Hydraulic and osmotic pressure ranges in the process
    [0124]
    [0127] In the third phase of OISO, the content of tank 1 (Stage I = 1) with a concentration of less than 10 g / l of NaCl (in this application example 9 g / l), is filtered in a conventional reverse osmosis unit operating at low pressure (unit AM in the description of the invention), in order to obtain a water with a low content of total dissolved solids, which would constitute the recovered product water. The rejection of salts from this last phase is recycled to one or more of the osmotic solute deposits, depending on their solids balance.
    权利要求:
    Claims (17)
    [1]
    1. System for the concentration of aqueous solutions with water recovery characterized in that it comprises:
    • at least one reverse osmosis module (OIM) comprising a concentrate side, a permeate side and a plurality of membranes;
    • at least one first tank (I) containing a first osmotic solution, where the first tank (I) is configured to concentrate the first osmotic solution from an initial concentration (Cii) to a final concentration (Cif), greater than the concentration initial (Cii), due to the passage of said first osmotic solution through the concentrate side of the at least one reverse osmosis module (OIM);
    • at least one second tank (I-1) containing a second osmotic solution, where the second tank (I-1) is configured to dilute the second osmotic solution from an initial concentration (Ci-1i) to a first final concentration ( Ci-1f), less than the initial concentration (Ci-1i), due to the passage of said second osmotic solution through the permeate side of the at least one reverse osmosis module (OIM);
    where the at least one reverse osmosis module (OIM) is configured to carry out the permeation of a difference in mass of water (Me-Ms) corresponding to the difference between an initial mass of water (Me) in the first tank ( I) and a mass of water outlet (Ms) from the first reservoir (I) due to the concentration of the first osmotic solution from the initial concentration (Cii) to the first final concentration (Cif);
    where the at least second reservoir (I-1) is also configured to concentrate the second osmotic solution from the first final concentration (Ci-1f) to a second final concentration (Ci-1f), greater than the first final concentration (Ci- 1f), due to the passage of said second osmotic solution through the concentrate side of the at least one reverse osmosis module (OIM), and
    where the system also includes:
    • at least one third reservoir (I-2) containing a third osmotic solution, where the third reservoir (I-2) is configured to dilute the third osmotic solution from an initial concentration (Ci-2i) to a first final concentration ( Ci-2f), lower than the initial concentration (Ci-2i), due to the passage of said third osmotic solution through the permeate side of the at least one reverse osmosis module (OIM), and
    where the at least one reverse osmosis module (OIM) is also configured to carry out the permeation of a water mass difference (Me'-Ms ') corresponding to the difference between an initial water mass (Me') in the second tank (I-1) and a mass of water outlet (Ms') from the second tank (I-1) due to the concentration of the second osmotic solution from the first final concentration (Ci-1f) to a second concentration final (Ci'1f ').
    [2]
    2. System for the concentration of aqueous solutions with water recovery according to claim 1, characterized in that it also comprises:
    • at least one initial reservoir (M) containing a saline solution, where the initial reservoir (M) is configured to concentrate the saline solution from an initial concentration (CMi) to a final concentration (CMf), greater than the initial concentration ( CMi), due to the passage of said saline solution on the concentrate side of the at least one reverse osmosis module (OIM) and to transfer to the first tank I the difference (MeM-MsM) between an initial mass MeM of the at least one tank initial (M) and final mass (MsM) of the at least one initial deposit (M);
    where the first tank (I) is also configured to dilute the first osmotic solution from the initial concentration (Cii) to the first final concentration (Cif), less than the initial concentration (Cii), due to the passage of said first osmotic solution through the permeate side of the at least one reverse osmosis module (OIM).
    [3]
    3. System for the concentration of aqueous solutions with water recovery according to claim 2, characterized in that it also comprises a pump (B) configured to pressurize the first osmotic solution contained in the first tank (I) I or the second tank I-1 depending on of the sequential transfer of water, or of the saline solution contained in the initial tank (M) to a first hydraulic pressure (Pf) prior to its passage through the concentrate side of the at least one reverse osmosis module (OIM).
    [4]
    4. System for the concentration of aqueous solutions with water recovery according to any of the preceding claims, characterized in that the at least one reverse osmosis module (OIM) is also configured to send to the second tank (I-1), the difference of mass of water (Me-Ms) corresponding to the difference between an initial mass of water (Me) in the first tank (I) and an outlet mass of water (Ms) from the first tank (I).
    [5]
    5. System for the concentration of aqueous solutions with water recovery according to any of the preceding claims, characterized in that the at least one reverse osmosis module (OIM) is also configured to send the mass difference to the third tank (I-2) of water (Me'-Ms') corresponding to the difference between an initial mass of water (Me ') in the second tank (I-1) and an outlet mass of water (Ms') from the second tank (I-1 ).
    [6]
    6. System for the concentration of aqueous solutions with water recovery according to any of the preceding claims, characterized in that the permeate side of the at least one reverse osmosis module (OIM) is arranged in countercurrent or isocurrent with the concentrate side of the al minus one reverse osmosis module (OIM).
    [7]
    System for the concentration of aqueous solutions with water recovery according to any of the preceding claims, characterized in that it also comprises a membrane refining unit (AM) configured to filter the content of the third tank (I-2).
    [8]
    8. System for the concentration of aqueous solutions with water recovery according to any of the preceding claims, characterized in that it comprises at least a fourth tank, so that the second tank (I-1) becomes the third tank (I-2) and the third deposit (I-2) becomes the fourth deposit.
    [9]
    9. System for the concentration of aqueous solutions with water recovery according to any of the preceding claims, characterized in that it comprises a control device configured to adjust the mass differences corresponding to the difference (Me-Ms) between the initial mass to desired values. of water (Me) in the first tank (I) and the final mass of water (Ms) of the first tank (I) and the difference (Me'-Ms ') between the initial mass of water (Me') in the second tank (I-1) and the final mass of water (Ms') of the second tank (I-1).
    [10]
    10. System for the concentration of aqueous solutions with water recovery according to claims 2 and 9 characterized in that the control device is also configured to adjust the mass difference (MeM-MsM) between the initial mass (MeM) of the at least one initial deposit (M) and the final mass (MsM) of the at least one initial deposit (M).
    [11]
    11. System for the concentration of aqueous solutions with water recovery according to any of claims 3 and 10, characterized in that it comprises:
    • a set of pipes for the main lines, recirculations and purges, as well as valves;
    • a set of instruments, among which conductometers, level meters and flow meters can be found, not being limited to them;
    • a set of separating elements configured to compartmentalize and separate the inlet and outlet streams of the tanks;
    where the control device controls a flow rate and a pressure of the pumps (B) and the set of valves and the set of instruments to operate the plurality of membranes and the at least one reverse osmosis module (OIM).
    [12]
    12. Procedure for the concentration of aqueous saline solutions with recovery of water carried out in the system of any of the preceding claims, characterized in that the procedure comprises the following steps:
    • at least a first stage where the concentration of a first osmotic solution is carried out in the at least one first reservoir (I) from an initial concentration (Cii) to a final concentration (Cif), greater than the initial concentration (Cii ), due to the passage of said first osmotic solution through the concentrate side of the at least one reverse osmosis module (OIM);
    • at least one second stage where the dilution of a second osmotic solution is carried out in the at least one second tank (I-1) from an initial concentration (Ci-1i) to a first final concentration (Ci-1f), lower than the initial concentration (Ci-1i), due to the passage of said second osmotic solution through the permeate side of the at least one reverse osmosis module (OIM);
    • at least a third stage where the permeation of a water mass difference (Me-Ms) is carried out in the at least one reverse osmosis module (OIM), water mass difference (Me-Ms) corresponding to the difference between an initial mass of water (Me) in the first tank (I) and an outlet mass of water (Ms) from the first tank (I) as a consequence of the at least one first stage;
    • at least a fourth stage where the concentration of the second osmotic solution is carried out in the at least one second tank (i-1) from the first final concentration (Ci-1f) to a second final concentration (C '"Y ), greater than the first final concentration (Ci-1f), due to the passage of said second osmotic solution on the concentrate side of the at least one reverse osmosis module (OIM);
    • at least a fifth stage where the dilution of a third osmotic solution is carried out in at least a third tank (I-2) from an initial concentration (Ci-2i) to a first final concentration (Ci-2f), lower that the initial concentration (Ci-2i), due to the passage of said third osmotic solution through the permeate side of the at least one reverse osmosis module (OIM);
    • at least one sixth stage where the permeation of a water mass difference (Me'-Ms ') is carried out in the at least one reverse osmosis module (OIM), mass difference (Me'-Ms') corresponding to the difference between an initial mass of water (Me ') in the second tank (I-1) and a mass of water outlet (Ms') from the second tank (I-1), as a consequence of the at least fourth stage.
    [13]
    13. Procedure for the concentration of aqueous saline solutions with water recovery according to claim 12, characterized in that it also comprises:
    • at least a seventh stage where the concentration of a saline solution is carried out in the initial tank (M), from an initial concentration (CMi) to a final concentration (CMf), greater than the initial concentration (CMi), due to to the passage of said saline solution through the concentrate side of the at least one reverse osmosis module (OIM);
    • at least an eighth stage of transfer to the at least first deposit I of the difference (MeM-MsM) between an initial mass MeM of the at least one initial deposit M and a final mass MsM of the at least one initial deposit M; and
    • at least a ninth stage where the dilution of the first osmotic solution is carried out in the first tank (I), from the initial concentration (Cii) to the first final concentration (Cif), lower than the initial concentration (Cii) , due to the passage of said first osmotic solution through the permeate side of the at least one reverse osmosis module (OIM).
    [14]
    14. Procedure for the concentration of aqueous saline solutions with water recovery according to claim 13, characterized in that it comprises at least a tenth stage where the pumping and pressurization of the first osmotic solution contained in the first tank (I) is carried out in the pump or the saline solution contained in the initial tank (M) up to a first hydraulic pressure (Pf) prior to its passage through the concentrate side of at least one reverse osmosis module (OIM).
    [15]
    15. Method for the concentration of aqueous saline solutions with water recovery according to any of claims 12 to 14 characterized in that it comprises at least an eleventh stage where the at least one reverse osmosis module (OIM) sends to the second tank, the difference in mass of water (Me-Ms) corresponding to the difference between the initial mass of water (Me) in the first tank (I) and the mass of water outlet (Ms) of the first tank (I).
    [16]
    16. Procedure for the concentration of aqueous saline solutions with water recovery according to any of claims 12 to 15, characterized in that it comprises at least a twelfth stage where the at least one reverse osmosis module (OIM) sends the difference in mass to the third tank of water (Me'-Ms') corresponding to the difference between the initial mass of water (Me ') in the second tank (I-1) and the mass of water outlet (Ms') of the second tank (I-1 ).
    [17]
    17. Method for the concentration of aqueous saline solutions with water recovery according to any of claims 12 to 16, characterized in that it comprises a final filtering stage to refine the content of the third tank (I-2).
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    同族专利:
    公开号 | 公开日
    ES2779982B2|2021-01-04|
    WO2020169858A1|2020-08-27|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US20120037566A1|2010-08-16|2012-02-16|Board of regents of the Nevada System of Higher Education, on Behalf of the University of|Osmotically-assisted desalination method and system|
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