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    • 专利摘要:
    POWER GENERATION PLANT, POWER PRODUCTION METHOD AND ZERO LIQUID DISCHARGE METHOD The invention relates to the ecologically correct deposition of salt by-product from zero liquid discharge desalination plant and sustainable development of brackish water resources interior. The plant comprises a salinity gradient power unit (60) with a high salinity supply, a low salinity supply and a mixed water outlet; wherein said high salinity feed comprises a rehydrated high salinity outlet from a zero liquid discharge desalination plant (20); wherein said mixed water outlet is directed to a body of water.
    公开号:BR112012013395B1
    申请号:R112012013395-0
    申请日:2010-11-04
    公开日:2020-07-21
    发明作者:Neil Edwin Moe
    申请人:Bl Technologies, Inc.；
    IPC主号:
    专利说明:

    [0001] [001] The invention relates to the ecologically correct deposition of salt by-product from zero liquid discharge desalination plant and sustainable development of indoor brackish water resources. BACKGROUND OF THE INVENTION
    [0002] [002] Desalination technologies typically operate by dividing a single aqueous feed stream into two outlet streams: a product whose properties are adapted for end use (such as drinking water), and a residual stream that contains most of the salts (and other contaminants) in high concentration. Currently, the deposition of high salinity desalination streams has significant problems, especially for indoor brackish water desalination units, and is considered the greatest impediment to the implementation of desalination technologies. Discharging the residual high salinity stream back into the environment inevitably results in an increase in the salinity of local water sources or those downstream, so it is evidently not sustainable. The sequestration of the high salinity by-product by injection into deep wells is limited to specific geographic regions and is characterized by high cost and uncertainty about the eventual destination of the high salinity liquid (for example, leaching will occur over time to the water supply underground ).
    [0003] [003] There has been a lot of recent activity around "Zero Liquid Discharge" technologies (ZLD - Zero Liquid Discharge) that operate in high salinity residual currents for desalination. These technologies allow for enhanced water recovery and reduce desalination by-products to aqueous slurries or solid salts. Today, ZLD technologies rely on expensive, energy-intensive thermal units, such as brine concentrators and crystallizers, or land-intensive evaporation ponds. Recent and near-future technological developments reduce the cost of ZLD by reducing the size of thermal units, as shown in the ZLD scenario tables below. Currently, in the United States, ZLD is practiced by around 120 industrial facilities, most of which are power plants. Local authorities have yet to adopt ZLD, but this picture is on the verge of change, as there is a convergence with the increase in water scarcity and the decreasing cost of ZLD.
    [0004] [004] However, despite significantly reducing the volume of the desalination by-product, the ZLD does not solve the final deposition problem, which remains significant. For example, a large brackish water desalination plant that treats 100,000 m3 / day of 2,000 ppm salt water produces about 200 metric tons of salt waste per day, or more likely if chemical softening processes are used. The landfill cost of salt at $ 50 per ton would be $ 10,000 per day, or $ 3,500,000 per year. In addition to the high cost, the landfill does not qualify as a sustainable solution because of the increasing use of land and the possibility of leaching.
    [0005] [005] The sustainable solution for interior desalination is to find uses for its by-product, transforming current waste into valuable products. In fact, processes have been developed to extract relatively pure salts such as magnesium hydroxide, calcium carbonate, and sodium chloride from high salinity desalination streams. However, extraction processes tend to be complex and costly, and markets for salts produced at necessary scales may not exist or can become saturated quickly. As a result, there remains a need to eliminate cost-effective and environmentally friendly disposal or reuse methods for the high-salinity desalination stream of zero liquid discharge desalination plants.
    [0006] [006] Another historically low-value stream is effluent from municipal wastewater treatment plants (WWTP). After primary and secondary treatment, most of the municipal wastewater is reinjected back into the environment. In coastal regions, canals are typically placed on (or under) the seabed and carry the effluent for several hundred meters or even kilometers on the high seas. Such discharges into the ocean are of particular environmental concern because of the large difference in salinity and density between municipal wastewater (typically 500 to 2,000 ppm) and seawater (typically 30,000 to 50,000 ppm). Discharges of wastewater create low-density plumes, low-salinity water that can be locally destructive and must be managed carefully.
    [0007] [007] The scale of deposition of contemporary wastewater in the sea is enormous, as two examples given below will confirm. The first is the Joint Water Pollution Control Plant (JWPCP), a large wastewater treatment plant on the west coast of the United States. JWPCP provides primary and secondary treatment for the collective wastewater of 3.5 million Los Angeles County residents before ejecting effluent into the Pacific Ocean (see http://www.lacsd.org/about/wastewater_facilities/jwpcp/ default.asp). The volume of this current is 1.14x106 m3 / day, or approximately ten times the capacity of the largest desalination plant in the United States. The outflow from JWPCP comprises about 20% of the total discharge of water served to the Southern California sea. The second example is the city of Singapore, where in 2006, 1.4x106 m3 / day of wastewater was treated by the Public Utilities Board (PUB) at various facilities, and 1.2x106 m3 / day was discharged ( see http://www.pub.gov.sg/). The scale of the discharges is directly related to the low value attributed to wastewater and the difficulty in finding suitable and accessible applications for large quantities of recycled water.
    [0008] [008] Recycled wastewater has increasingly become an important water resource usable in regions that suffer from water scarcity, and there are many initiatives being discussed or implemented to increase recycling and reuse. However, there are natural limits associated with the amount of water served that can be recycled and effectively reused. First, the demand for substandard water is limited to applications such as construction sites, irrigation, or certain industrial uses. The infrastructure for distribution must be established, which can be costly. On the other hand, the advanced tertiary treatment technology required to improve the quality of secondary effluent for indirect potable reuse, such as groundwater recharge, is costly, and again the distribution infrastructure needs to be built. Even with investment in such expensive tertiary treatment technology, public resistance to perceiving recycling projects "from the private to the tap" has been great; therefore, the need for less expensive and less controversial means to extract value from municipal wastewater persists.
    [0009] [009] It is known that the power of the salinity gradient can be produced by different approaches, with the use of high and low salinity contrast currents. The two most well-known power generation processes are membrane-based, called pressure-delayed osmosis (PRO - Pressure Retarded Osmosis) and reverse electrodialysis (RED - Reverse Electrodialysis). PRO and RED are described in the following patent publications of US No. 7,563,370, US 4,193,267, US 4,171,409, US 3,906,250 and US 2006 / 0196836A1, each of which is incorporated by reference in this document. . Although pilot-scale demonstrations of both PRO and RED are ongoing in Europe, no technology has been commercially deployed. The application to be considered in these pilot studies is the use of the difference in salinity between rivers and oceans to generate power in the estuaries. The commercial viability of PRO and RED depends on the ability to generate the greatest amount of power with the use of the smallest membrane area. Unfortunately, most analyzes of the power generation potential of river / ocean water using currently available membranes show that the cost of membranes needs to be utopically low in order for the process to be economically viable. The greater difference in salinity between high and low salinity currents and more effective membranes that have greater permeability would improve the commercial outlook. DESCRIPTION OF THE INVENTION
    [0010] [0010] The present invention relates to a power generation plant, comprising the salinity gradient power unit (SGPU - Salinity Gradient Power Unit) comprising the high salinity supply, the low salinity supply, and the mixed water outlet. The high salinity feed is a by-product of a ZLD operation. The mixed water outlet is emptied into a body of water. BRIEF DESCRIPTION OF THE DRAWINGS
    [0011] [0011] Figure 1 represents an indoor brackish water desalination unit (BWDU - Brackish Water Desalination Unit) and dehydration unit layout that results in ZLD.
    [0012] [0012] Figure 2 represents a SGPU and a hydration arrangement according to the present invention.
    [0013] [0013] Figures 3a to 3e represent alternative SGPU and hydration arrangements according to the present invention.
    [0014] [0014] Figure 4 represents a PRO disposition unit according to the present invention.
    [0015] [0015] Figure 5 represents a RED disposition unit according to the present invention.
    [0016] [0016] Figure 6 represents a hydrator used to combine high and low salinity water for flushing.
    [0017] [0017] Figure 7 shows the power of thermodynamic benefit generated by mixing a 1 m3 / s of low salinity current (concentration set at 500 ppm) with a high salinity current (15,000 to 160,000 ppm) to produce mixing water (10,000 to 48,000 ppm).
    [0018] [0018] Figure 8 shows the power of thermodynamic benefit generated per cubic meter of total water used in the process (equal to the volume of the mixing water stream) as functions of high salinity concentrations (15,000 to 160,000 ppm) and the mixing water stream (10,000 to 48,000 ppm), which sets the concentration of the low salinity stream to 500 ppm.
    [0019] [0019] Figure 9 shows the thermodynamic benefit power generated per metric ton of salt present in the high salinity stream as a function of the concentrations of the high salinity stream (15,000 to 160,000 ppm) and the mixing water stream (10,000 to 48,000 ppm), which sets the concentration of the low salinity current to 500 ppm.
    [0020] [0020] Figure 10 shows the power of thermodynamic benefit generated by mixing a low salinity current of 1 m3 / s (500 to 32,000 ppm) with a high salinity current (15,000 to 96,000 ppm) to produce water of mixing (10,000 to 48,000 ppm), where the ratio of high volume salinity to low volume salinity is set to 1. DESCRIPTION OF ACCOMPLISHMENTS OF THE INVENTION
    [0021] [0021] The invention will now be described with reference to the drawings, in which preferred embodiments are described in detail to enable the practice of the invention. Although the invention is described with reference to such specific preferred embodiments, it will be understood that the invention is not limited to such preferred embodiments. On the contrary, the invention includes numerous alternatives, modifications, and equivalents as will be made apparent from consideration of the detailed description below.
    [0022] [0022] Referring now to the drawings, Figure 1 shows an interior BWDU 20 that desalinates water taken from a salt water body 10 and produces both usable water and a high salinity outlet. In ZLD processes, the high salinity outlet can be further treated in a dehydrator 30 that removes usable water from the high salinity outlet and dehydrates the residue from the high salinity outlet. Part of the usable water produced by the dehydrator 30 is drinking water. In one embodiment, it is contemplated that the dehydrator 30 consists of a brine evaporator unit that concentrates the salts and a crystallizer unit or evaporation tank to recover or expel the remaining water. The salinity level of the usable water is generally less than or equal to 500 ppm, and the high salinity output is solid salts or sludge. The dehydrated high salinity outlet is then transported out of hydrator location 40 in a SGPU 60, as shown in Figure 2. The dehydrated high salinity outlet can be transported using a variety of methods, including by truck , train, boat or channel.
    [0023] [0023] In Figure 2, the dehydrated high salinity outlet is rehydrated in hydrator 40. In one embodiment, low salinity water is used to rehydrate the dehydrated high salinity outlet. The rehydrated high salinity outlet is fed to the SGPU and used as the high salinity feed. Low salinity water is also fed to the SGPU and used as the low salinity feed. In the preferred embodiment, such a low salinity feed is the secondary effluent from a WWTP 50. It is contemplated that in some embodiments river water can be used as the low salinity feed. Additionally, it is contemplated that in some embodiments the auxiliary high salinity inlet of the hydrator 40 can be used to rehydrate the high salinity outlet dehydrated with high salinity liquids, including brine, such as the concentrated stream of a seawater from a power plant. desalination, or sea water.
    [0024] [0024] In addition, the fluid rates of the low salinity feed provided for SGPU 60, the low salinity water provided for hydrator 40, the auxiliary high salinity inlet provided for hydrator 40, and the high salinity outlet rehydrate supplied for SGPU 60 are adjustable.
    [0025] [0025] The adjustable water flow rate for hydrator 40, along with pH and temperature, can be used to control the salinity level of the rehydrated high salinity outlet. The high salinity outlets that have different compositions can be mixed in order to control the concentrations of individual ions within the rehydrated high salinity outlet. The fluid rates of the rehydrated high salinity outlet and low salinity feed entering the high salinity stream on the SGPU 60 control the salinity level of the SGPU 60 mixed water outlet. The required salinity level of the mixed water outlet varies depending on the salinity of the body of water in which it empties. In certain cases it is desirable that the salinity and density of the mixing water are substantially equivalent to that of the receiving water body; in other cases it is desirable that the salinity and density of the mixing water be lower than that of the receiving water body in order to maintain positive buoyancy. For realizations that use WWTP 50 secondary effluent as the low salinity feed, adding salt to the secondary effluent will increase its concentration and density and can make the discharge more environmentally friendly.
    [0026] [0026] Figure 3a represents a case in which the low salinity feed exceeds SGPU 60 and dilutes the mixed water outlet before discharge. In this embodiment, the WWTP 50 secondary effluent is used with the SGPU 60 low salinity feed and hydrates the dehydrated high salinity outlet. Figure 3b represents an embodiment in which river water is used as the low salinity feed of SGPU 60 and hydrates the dehydrated high salinity outlet in hydrator 40.
    [0027] [0027] Figure 3c represents an embodiment in which the secondary effluent from a WWTP 50 is used as the low salinity feed of SGPU 60, and river water is used to hydrate the dehydrated high salinity outlet in hydrator 40. As you can see To be seen, a path is provided so that it allows a combination of secondary effluent from a WWTP 50 and river water to be used in the SGPU 60 low salinity feed and to hydrate the dehydrated high salinity outlet.
    [0028] [0028] Figure 3d represents an embodiment in which the secondary effluent from a WWTP 50 is used as the low salinity feed of SGPU 60, and the concentrated current from a seawater desalination plant is used to hydrate the outlet of high salinity dehydrated in hydrator 40.
    [0029] [0029] Figure 3e represents an embodiment in which the secondary effluent of a WWTP 50 is used as the low salinity feed of SGPU 60, and ocean water is used to hydrate the dehydrated high salinity outlet in the hydrator 40.
    [0030] [0030] Figure 4 represents a PRO 70 unit arranged so that it can be used in the SGPU. In the PRO 70 unit, a vessel 80 is shown divided into a pressurized high salinity chamber 90 and a depressurized low salinity chamber 100. The high salinity supply is directed to the high salinity chamber 90, while the low salinity supply is directed to the low salinity chamber 100. The two chambers are separated by a semipermeable membrane 110 which allows the contents of the low salinity chamber 100 to penetrate the high salinity chamber 90, while retaining the contents of the high salinity chamber 90. A difference in hydraulic pressure between the liquids on the opposite faces of the membrane 110 is less than the difference in osmotic pressure between the liquids. The difference in chemical potential between the contents of the high salinity chamber 90 and the low salinity chamber 100 causes the transport of water from the low salinity chamber 100 to the high salinity chamber 90 and pressurization of the volume of water transported, which is converted to electrical power by a hydroturbine 120. The application of hydrostatic pressure to the outlet of rehydrated high salinity will partially delay the transport of water. The water flowing from the high salinity chamber 90 to the hydroturbine 120 is a mixture of low salinity feed and high salinity feed. The power output of the PRO 70 unit is influenced by the difference in osmotic pressure between the two solutions, the relative fluid rates of the two inlet currents, the temperature, the hydraulic pressure, and the membrane properties. The water that leaves hydroturbine 120 is directed to the mixed water outlet of SGPU.
    [0031] [0031] The power generation capacity of the PRO 70 unit increases at higher water temperatures due to the driving force of the increased osmotic pressure and the increased membrane permeability. Residual heat as well as the by-product of power generation can be advantageously used to heat the low salinity supply and / or high salinity supply to increase the output power of the PRO 70 unit and make better use of existing energy resources.
    [0032] [0032] Figure 5 represents a RED 120 unit arranged so that it can be used in the SGPU. In the RED 120 unit, cationic membranes (CM - Cation Membranes) 140 and anionic membranes (AM - Anion Membranes) 130 are arranged in an alternating sequence, which in turn produces high salinity compartments and low salinity compartments. The high salinity feed is directed towards the high salinity compartments, while the low salinity feed is directed towards the low salinity compartments. Since the concentration of salt ions in the high salinity compartments is higher than the ions in the low salinity compartments, the sodium cations diffuse from the high salinity compartments through the CM 140 to the low salinity compartments. In addition, the chloride anions of the high salinity compartments diffuse through the AM 130 to the low salinity compartments. This separation of charges produces a difference in chemical potential on each membrane that can be used directly as electrical energy through the electrical voltage invoked through the anode and cathode and then an electrical current through an electrical charge. The total electricity production capacity of the RED 120 unit is determined by a number of factors including numerous membranes in the stack, the absolute temperature and the ratio of solution concentrations in the low and high salinity compartments, the internal resistance of the RED 120 unit, and the electrode properties. The water outlet from the low and high salinity compartments mixes and makes the SGPU water outlet mixed.
    [0033] [0033] The power generation capacity of the RED 120 unit increases at higher water temperatures due to greater ion mobility and decreases the resistance in the solution chambers. Residual heat such as the by-product of power generation can be advantageously used to heat the low salinity supply and / or high salinity supply to increase the output power of the RED 120 unit and make better use of existing energy resources.
    [0034] [0034] Figure 6 represents a configuration in which the dehydrated high salinity outlet is rehydrated in a hydrator 40 and the mixing water is discharged from the hydrator 40 into a receiving water body. Such a configuration can be useful during SGPU construction or when the SGPU is disconnected. In one embodiment, the low salinity feed is used to rehydrate the dehydrated high salinity outlet. In the preferred embodiment, this low salinity feed is the secondary effluent of a WWTP 50. It is contemplated that in some embodiments, river water can be used as the low salinity feed. Additionally, it is contemplated that in some embodiments, the high salinity brine, such as the concentrated stream from a seawater desalination plant, or seawater can be used to rehydrate the dehydrated high salinity outlet through the auxiliary water inlet. high salinity of the hydrator 40. In addition, it is contemplated that some achievements rehydrate the dehydrated high salinity output with the use of a combination of two or more among: river water, high salinity brine, or sea water.
    [0035] [0035] The adjustable water flow rate in hydrator 40, together with pH and temperature, can be used to control the salinity level of the rehydrated high salinity outlet. The high salinity outlets that have different compositions can be mixed in order to control the concentrations of individual ions within the rehydrated high salinity outlet. The level of salinity of the required mixed water outlet varies depending on the salinity of the body of water into which it is emptied. In certain cases, it is desirable that the salinity and density of the mixing water are equivalent to that of the receiving water body; in other cases it is desirable that the salinity and density of the mixing water be lower than that of the receiving water body in order to maintain positive buoyancy. In other cases, it is desirable that the salinity of the mixing water does not exceed the salinity of the receiving water body by more than 3%. For achievements using WWTP secondary effluent for low salinity feed, adding salt to the secondary effluent will increase its concentration and density, and may make the discharge more environmentally friendly. EXAMPLE CALCULATIONS
    [0036] [0036] The amount of energy generated from a mixing process can be estimated using the theory of the ideal solution, which is described in several physicochemical books. For the purpose of these calculations, the specific example of Post et al. It is followed (Post, Veerman, Hamelers, Euverink, Metz, Nymeijer, Buisman, "Salinity-Gradient Power: Evaluation of Pressure-Retarded Osmosis and Reverse Electrodialysis", Journal of Membrane Science, volume 228, pages 218 to 230, 2007). Free energy is available from mixing a concentrated solution with a diluted solution and is taken from equation 3 in this reference:
    [0037] [0037] Subscriptions c, d, and m refer to concentrated, diluted, and mixed solutions respectively. Subscript i refers to the number of components (two in this case: NaCI and water). V is the volume of solution (for example, in m3), c is the concentration (mol / m3), and x is the molar fraction. For salt, the concentration of sodium + chloride ions is twice the concentration of NaCI. R is the constant gas and T is the absolute temperature. Following Post et al., The empirical density of sodium chloride solutions as a function of salt concentration at T = 20 ° C (T = 293 K) was used (RC Weast, ed., CRC Handbook of Chemistry and Physics, 66 ° Edition (1985 to 1986), CRC Press, Inc., Boca Raton, Florida pages D to 253 to 254.) to define the volume of solutions. The equation for free energy above represents the behavior of ideal solutions; the comparison with empirical thermodynamic data indicates that predicted results are only about 10% too high, except at the highest salt concentrations. At this point, an ideal solution approach underestimates the mixing energy. (M.E. Guendouzi, A. Dinane, A. Mounir, "Water activities, osmotic and activity coefficients in aqueous chloride solutions at T = 298.15 K by the hygrometric method", J. Chem. Thermodynamics 33 (2001) 1059-1072.). The change in free energy is the thermodynamic benefit of the process; the actual amount of energy recovered by a practical device will depend on the details of the system and process design, but 50% of the effectiveness is not an immoderate assumption for initial estimation purposes.
    [0038] [0038] Figure 7 shows the power of thermodynamic benefit generated from a mixture of 1 m3 / s of low salinity current (concentration set at 500 ppm) with a high salinity current (15,000 to 160,000 ppm) to produce water mixing (10,000 to 48,000 ppm). Mixing ratios are varied as needed. Two general trends can be seen from this data. First, power generation always increases as the salt concentration in the high salinity stream rises. This is because the mixing energy rises with the increase in the difference in concentrations between the high and low salinity currents. Second, the higher concentrations of water output mixed by SGPU result in higher power output per unit of low salinity feed inlet volume.
    [0039] [0039] Figure 8 shows the power of thermodynamic benefit generated per cubic meter of total water used in the process, (equal to the volume of the mixing water stream,) the functions of concentrations of the high salinity stream (15,000 to 160,000 ppm ) and the mixing water stream (10,000 to 48,000 ppm), setting the concentration of the low salinity stream to 500 ppm. Interestingly, the power produced at moderately low concentrations of the high salinity stream (50,000 to 70,000 ppm) is almost independent of the target composition of the mixed water outlet stream. At higher concentrations of high salinity current, the amount of power produced again with a tendency to concentrate the mixed water outlet stream.
    [0040] [0040] Figure 9 shows the thermodynamic benefit power generated per metric ton of salt present in the high salinity stream as a function of the concentrations of the high salinity stream (15,000 to 160,000 ppm) and the mixing water stream (10,000 to 48,000 ppm), setting the concentration of the low salinity current to 500 ppm. Once again, the trend is observed that the amount of power generated increases as the salt concentration in the high salinity stream rises. On the other hand, the amount of energy extracted from a given amount of salt increases as the target salinity of the mixed water outlet stream decreases. This is because the mixing energy continues to increase under continued dilution of a concentrated stream. The greatest dilution results in greater energy production, but requires more water.
    [0041] [0041] Figures 7 to 9 taken together suggest that two general operating strategies exist for a SGPU. The first aims to completely minimize the use of water by defining the target concentration of the mixed water outlet stream to be high. This will also be the low cost of capital option as the difference in concentration between the high and low salinity currents (and the driving force for mixing) is maximized through the process. The high driving force results in higher power productivity per unit area of membrane. The second operational strategy aims to extract as much energy as possible from the salt in the high salinity stream by allowing the dilution to proceed as it is practiced. Preferably, the mixing water concentration should be greater than 5,000 ppm. This strategy will maximize the amount of power generated from a limited amount of salt, but the cost of capital and the size of the system will be greater because the driving force for mixing is necessarily capable of declining. In both strategies, raising the concentration of the high salinity stream as high as possible is beneficial in principle.
    [0042] [0042] Figure 10 shows the thermodynamic benefit power generated from a mixture of 1 m3 / s of low salinity current (500 to 32,000 ppm) with a high salinity current (15,000 to 96,000 ppm) to produce water of mixture (10,000 to 48,000 ppm), where the mixing ratio of high salinity current volume / low salinity current volume is set to 1. In contrast to the calculations shown in Figures 7 to 9, the concentration of the low current salinity is varied, rising from 500 to 32,000 ppm. The amount of power decreases as the salinity of the low-salinity current rises, as it reduces the difference in concentration between low and high salinity currents. For the salinity ranges in municipal wastewater streams (500 to 2,000 ppm), the effect is not very large, but if the concentration of the low salinity stream increases too much (greater than 10,000 ppm), productivity drops significantly. The use of sea water (32,000 ppm) for the diluted stream is unlikely to be viable in any situation. (Preferably, the salinity ratio between low and high salinity currents should be greater than 5: 1).
    [0043] [0043] Typical municipal wastewater salinity is in the range of 500 to 2,000 ppm, compared to ocean salinity of 30,000 to 50,000 ppm. The capacity of municipal wastewater discharges to absorb salt is immense. A hypothetical discharge of one million cubic meters per day in a concentration of 500 ppm of salt in seawater with a concentration of 30,000 ppm would require 29,500 tons / day of salt to complete the "neutralization." Continuing the example of interior desalination of the introduction, (100,000 m day, 2,000 ppm of brackish water in salt concentration, 200 tons / day salt produced from ZLD), it would be shown that the municipal wastewater treatment plant in the regions coastal areas could absorb any reasonable amount of by-products for inland desalination processes. EXAMPLES COMPARATIVE EXAMPLE 1
    [0044] [0044] The calculations described above can be extended further to assess the practice scenarios. For example, as shown in Figure 3a, the location of the SGPU on the site of a large wastewater treatment plant near the ocean is considered. It is assumed that the volume of the treated wastewater stream is 1 million cubic meters per day and the salt concentration is 500 ppm. A portion of that stream is used to constitute the low-salinity stream, and the other portion is used to rehydrate the salt sent from interior ZLD desalination operations (the salt is presumed to be completely dry for simplicity), such that the concentration of the high salinity stream is 150,000 ppm. The three scenarios, which are adjusted to different concentrations of the mixed water outlet stream, are considered: 10,000, 32,000, and 48,000 ppm. In the event that the mixed water outlet stream is 48,000 ppm, a portion of the low-salinity stream is routed around the SGPU to dilute the seawater concentration (assuming it is 32,000 ppm). The results are given in Table 1.
    [0045] [0045] As shown in Figure 3e, one million cubic meters per day of stream of water is assumed to be the stream of low salinity, with a salt concentration of 500 ppm. Sea water (32,000 ppm) is used to rehydrate ZLD salt at 150,000 ppm. The three scenarios, adjusted at different concentrations of the mixed water outlet stream are considered: 10,000, 32,000, and 48,000 ppm. In the case of 48,000 ppm in the mixed water outlet stream, a portion of the low salinity stream is routed around the SGPU to dilute in the seawater concentration. The results are given in Table 2.
    [0046] [0046] As shown in Figure 3d, one million cubic meters per day of stream of water is assumed to be the stream of low salinity, with a salt concentration of 500 ppm. Concentrate from the seawater desalination plant (64,000 ppm) is used to rehydrate ZLD salt to 150,000 ppm. The three scenarios, adjusted at different concentrations of the mixed water outlet stream, are considered: 10,000, 32,000, and 48,000 ppm. In the case of 48,000 ppm in the mixed water outlet stream, a portion of the low salinity stream is routed around the SGPU to dilute in the seawater concentration (32,000 ppm). The results are given in Table 3.
    [0047] [0047] There are numerous advantages of a complete integrated approach to managing water resources as described in this invention. The solid benefits for an indoor desalination plant avoid the costs of a landfill and move a sustainable process in which the salt is completely removed from the local environment. This can be achieved by the process described in this invention without the complexity and cost associated with selective salt removal. Mixing salts perform as well as pure power generation species. In addition, the demand for potency is essentially infinite, in contrast to the market for pure salts. The solid benefit for wastewater treatment plants and coastal communities is an additional resource of clean power (which will not contribute to carbon dioxide emissions), with the added benefit of potentially greater compatibility of final mix water effluent with the sea water due to better combined salinity and density. The "neutralization" of low salinity wastewater with ZLD Salt does not carry the heavy costs of treatment of and / or distribution infrastructure often associated with wastewater recycling projects, and will not raise public issues associated with indirect drinking reuse. Furthermore, the present invention removes one of the greatest barriers to the commercial implementation of salinity potency by using ZLD salt to increase the concentration of the concentrated stream to a potential of many times the concentration of seawater (above 150,000 a 300,000+ ppm). This considerably increases the driving force for power generation, shrinking the membrane area and the cost of capital. An approach that balances indoor desalination, generation of salinity power, water conversion, and wastewater recycling represents maximizing the water value of regions or nations and power resources. Although this invention has been described in conjunction with the specific embodiments described above, it is evident that many alternatives, combinations, modifications and variations are evident to a person skilled in the art. As a consequence, the preferred embodiments of this invention, as defined above are intended to be illustrative only, and have no limiting sense. Various changes can be made without departing from the scope of this invention.
    权利要求:
    Claims (16)
    [0001]
    POWER GENERATION PLANT, characterized by comprising a salinity gradient power unit (60) with a high salinity supply, a low salinity supply and a mixed water outlet; wherein said high salinity feed comprises a rehydrated high salinity outlet from a zero liquid discharge desalination plant (20); wherein said mixed water outlet is directed to a body of water (10).
    [0002]
    POWER GENERATION PLANT, according to claim 1, characterized in that the salinity of the mixed water outlet does not exceed the salinity of the water body (10) by more than 3%
    [0003]
    POWER GENERATION PLANT, according to claim 1, characterized in that the salinity and density of the mixed water outlet are lower than the salinity and density of the water body (10).
    [0004]
    POWER GENERATION PLANT, according to claim 1, characterized by the low salinity supply comprising a secondary effluent from a wastewater treatment plant (50).
    [0005]
    POWER GENERATION PLANT, according to claim 1, characterized by the low salinity supply comprising river water from an estuary.
    [0006]
    POWER GENERATION PLANT, according to claim 1, characterized in that a secondary effluent from a wastewater treatment plant (50) is used to rehydrate the high salinity outlet.
    [0007]
    POWER GENERATION PLANT according to claim 1, characterized by river water from an estuary being used to rehydrate the high salinity outlet.
    [0008]
    POWER GENERATION PLANT, according to claim 1, characterized in that sea water is used to rehydrate the high salinity outlet.
    [0009]
    POWER GENERATION PLANT, according to claim 1, characterized in that a concentrated stream from a desalination plant (20) is used to rehydrate the high salinity outlet.
    [0010]
    POWER GENERATION PLANT, according to claim 1, characterized in that the salinity gradient power unit (60) additionally comprises a reverse electrodialysis unit (120).
    [0011]
    POWER GENERATION PLANT according to claim 1, characterized in that the salinity gradient power unit (60) additionally comprises a delayed pressure osmosis unit (70).
    [0012]
    POWER GENERATION PLANT, according to claim 1, characterized in that the mixed water outlet is combined with the low salinity feed before entering the water body (10).
    [0013]
    POWER PRODUCTION METHOD, characterized by understanding the steps of: providing a salinity gradient power unit (60); providing a dehydrated high salinity outlet from a zero liquid discharge desalination plant (20); supply a secondary effluent from a wastewater treatment plant (50); rehydrate the dehydrated high salinity outlet; feeding the salinity gradient power unit (60) with the rehydrated high salinity outlet as a high salinity feed; feeding the salinity gradient power unit (60) with secondary effluent from a wastewater treatment plant (50) as a low salinity feed; generate an electric current in the salinity gradient power unit (60); produce a mixed water outlet that is directed to a water body (10), in which the salinity of the mixed water outlet does not exceed the salinity of the water body (10) by more than 3%.
    [0014]
    METHOD, according to claim 13, characterized in that the temperatures of the low salinity and high salinity feeds are increased.
    [0015]
    METHOD according to claim 13, characterized in that the gradient power unit comprises a pressure delayed osmosis unit (70).
    [0016]
    ZERO LIQUID DISCHARGE DEPOSITION METHOD, characterized by understanding the steps of: providing a dehydrated high salinity outlet from a zero liquid discharge desalination plant (20); provide a low salinity feed; rehydrate the dehydrated high salinity outlet; producing a mixed water outlet comprising the low salinity feed and the rehydrated high salinity outlet; and direct the mixed water outlet to a body of water, where the salinity of the mixed water outlet does not exceed the salinity of the water body (10) by more than 3%.
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    同族专利:
    公开号 | 公开日
    AU2010326307B2|2016-03-24|
    CN102971531B|2016-08-31|
    US20110131994A1|2011-06-09|
    BR112012013395A2|2016-03-08|
    CY1118210T1|2017-06-28|
    EP2507515A2|2012-10-10|
    CA2782664C|2017-02-07|
    CA2782664A1|2011-06-09|
    ES2589778T3|2016-11-16|
    BR112012013395A8|2018-07-03|
    CN102971531A|2013-03-13|
    MX2012006416A|2012-10-15|
    US8695343B2|2014-04-15|
    EP2507515B1|2016-07-20|
    AU2010326307A1|2012-06-21|
    SG181483A1|2012-07-30|
    MX341542B|2016-08-23|
    WO2011068616A3|2013-04-18|
    WO2011068616A2|2011-06-09|
    IN2012DN04911A|2015-09-25|
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    法律状态:
    2019-01-02| B25A| Requested transfer of rights approved|Owner name: BL TECHNOLOGIES, INC. (US) |
    2019-01-08| B06F| Objections, documents and/or translations needed after an examination request according art. 34 industrial property law|
    2019-10-08| B06U| Preliminary requirement: requests with searches performed by other patent offices: suspension of the patent application procedure|
    2020-06-16| B09A| Decision: intention to grant|
    2020-07-21| B16A| Patent or certificate of addition of invention granted|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 04/11/2010, OBSERVADAS AS CONDICOES LEGAIS. |
    优先权:
    申请号 | 申请日 | 专利标题
    US12/631,248|2009-12-04|
    US12/631,248|US8695343B2|2009-12-04|2009-12-04|Economical and sustainable disposal of zero liquid discharge salt byproduct|
    PCT/US2010/055345|WO2011068616A2|2009-12-04|2010-11-04|Economical and sustainable disposal of zero liquid discharge salt byproduct|
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