WO2014090973A1 - Procédé et installation de traitement et transformation d'eaux - Google Patents

Procédé et installation de traitement et transformation d'eaux Download PDF

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Publication number
WO2014090973A1
WO2014090973A1 PCT/EP2013/076465 EP2013076465W WO2014090973A1 WO 2014090973 A1 WO2014090973 A1 WO 2014090973A1 EP 2013076465 W EP2013076465 W EP 2013076465W WO 2014090973 A1 WO2014090973 A1 WO 2014090973A1
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Prior art keywords
brine
plant
raw water
membrane
distillate
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PCT/EP2013/076465
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German (de)
English (en)
Inventor
Burkhard Seifert
Alexander Kroiß
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Technische Universität München
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Application filed by Technische Universität München filed Critical Technische Universität München
Publication of WO2014090973A1 publication Critical patent/WO2014090973A1/fr

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    • 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
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/048—Purification of waste water by evaporation
    • 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
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/14—Treatment of water, waste water, or sewage by heating by distillation or evaporation using solar energy
    • 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
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • 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
    • C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by 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
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/08—Seawater, e.g. for desalination
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/16—Nature of the water, waste water, sewage or sludge to be treated from metallurgical processes, i.e. from the production, refining or treatment of metals, e.g. galvanic wastes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/32—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/20—Controlling water pollution; Waste water treatment
    • Y02A20/208—Off-grid powered water treatment
    • Y02A20/212—Solar-powered wastewater sewage treatment, e.g. spray evaporation

Definitions

  • the present invention relates to a method and a plant for the treatment and processing of waters by removing a component to be separated at least partially from a raw water and / or recovered in concentrated form.
  • the method and the device are used in particular in the desalination or salt reduction of seawater or brackish water or in the treatment and processing of waters from the oil and gas industry or from mining.
  • the process and apparatus can provide permeate, very pure distillate, and very high concentration sols of a component to be separated.
  • raw water For the desalination of waters, for example of sea or brackish water, and for the treatment of industrial wastewater, it is customary in the prior art to use membrane processes and / or thermal processes to remove salt or other constituents to be separated from the water to be treated, hereinafter referred to as "raw water”. designated to remove.
  • the prior art uses various membrane processes for the treatment and processing of waters. Examples are the methods of reverse osmosis (RO), nanofusion and ultrafiltration. Ultrafiltration processes are used in particular in the oil and gas industry for the treatment of industrial waters.
  • RO reverse osmosis
  • nanofusion nanofusion
  • ultrafiltration processes are used in particular in the oil and gas industry for the treatment of industrial waters.
  • Membrane processes are widely used for desalination applications, for example in seawater or brackish water desalination, due to their comparatively good energy efficiency, which is usually between 2.5 and 10 kWh for the recovery of one m 3 of water.
  • membrane plants are also used for the treatment and processing of industrial waters, for example - -
  • waters from mining waters in electroplating or waters in the food industry.
  • certain waters are concentrated using membrane techniques.
  • a raw water to be treated is brought into contact with a membrane.
  • the membrane is largely impermeable to the constituents of the raw water to be separated (so-called semipermeable membrane), so that the part of the raw water flowing through the membrane (so-called permeate) is free or almost free of the components to be separated, while the effluent concentrate (so-called brine), which does not flow through the membrane containing these constituents.
  • a water recovered from the raw water and having a higher concentration of a component to be separated than the raw water is referred to as a "brine", irrespective of whether the component to be separated is a salt Not.
  • the concentration ofprooftren- nenden raw water constituents In the treatment of raw water with the help of reverse osmosis so the permeate exits on the outlet side of the membrane, while increasing in the brine, the concentration ofprooftren- nenden raw water constituents.
  • the brine or a portion thereof may be recycled to the entrance side of the membrane as often as necessary until a certain concentration of the component to be separated is reached on the entrance side of the membrane.
  • the ratio of the amount of permeate obtained to the amount of raw water used for this purpose is also referred to as the recovery ratio.
  • MeemassemmLiteosmose (MWUO) plants higher investment and operating costs than for reverse osmosis systems, which treat a raw water with a relatively low salinity.
  • thermal treatment processes include membrane distillation, mechanical vapor compression, multi-effect distillation (MED), wet-air distillation and multi-stage flash evaporation (so-called multi-stage flash, MSF).
  • MED multi-effect distillation
  • MSF multi-stage flash
  • thermal treatment processes can also be used for waters or tailings from the oil and gas industry, waters from mining, waters in electroplating or waters in the food industry.
  • certain waters are also concentrated or thickened using thermal treatment processes to produce sugar concentrate, thick juice or fruit juice concentrate.
  • Thermal treatment processes such as the moist air distillation, are relatively energy consuming and are used especially when an advantageous heat source for treatment and / or processing of raw water is present.
  • the raw water is heated or heated, whereby only pure water evaporates and humidifies the air in the system.
  • the water vapor is condensed out as pure distillate. What remains is a brine, which can be removed as waste or residue product.
  • it is also possible to use "virtually salt-free operation" so-called zero liquid discharge) in which the residue product is present in a very high concentration so that only a very small amount of brine has to be removed.
  • Feuchtluftdestillationsanlagen can be operated almost independently of the concentration of the components to be separated in the raw water. Therefore, they are particularly suitable for the treatment and processing of high saline raw water, since the plant configuration and the energy consumption are hardly affected by the salinity.
  • the prior art also discloses the combination of thermal processing systems with membrane systems.
  • Such a hybrid desalination system will be - -, in the article: "Hybrid Desalination Systems. Alternative Designs of Thermal and Membrane Processes" M. Marcovecchio et al, 10 th International Symposium on Process Systems Engineering - indicated PSE in 2009.
  • the system includes a first multi-stage Flash (MSF) system and a second reverse osmosis system.
  • the flash evaporation plant is connected upstream of the reverse osmosis system, which increases the throughput of the reverse osmosis plant.
  • a series connection of two membrane plants and a subsequent thermal see plant for the treatment of hot textile wastewater is known from DE 31216942 AI.
  • the two membrane plants form a first and a second plant stage and serve for the at least partial recovery of the thermal energy contained in the textile wastewaters.
  • the warm permeate of the second membrane unit has a lower temperature than the hot permeate of the first membrane unit and can be returned to the reprocessed hot textile waste water flowing to the first membrane unit for a renewed separation process.
  • the thermal plant forms a third stage for the recovery of recyclables by means of concentration.
  • the inventive method comprises feeding a raw water into a membrane plant, wherein the raw water contains a component to be separated.
  • the raw water is separated into at least one permeate and a first brine.
  • the permeate contains a smaller proportion of the component to be separated than the raw water.
  • the first brine contains a higher proportion of the component to be separated than the raw water.
  • the first brine is fed to a thermal plant, in which the first brine in at least - - a first distillate and a second brine is separated. At least part of the first distillate is introduced into the raw water, which is located in the inflow to or in the membrane plant. As a result, the concentration of a component to be separated in the raw water in the inflow to or in the membrane system is reduced.
  • seawater or brackish water may similarly refer to other raw waters having a corresponding concentration rather than a particular salinity have any other components to be separated, and all said in terms of seawater or brackish water desalination applies mutatis mutandis to other raw waters and components to be separated, especially for waters or fracking water from the oil and gas industry, for waters from mining, for water in the Electroplating or for waters in the food industry.
  • the costs for the plant itself and for the operation of the plant increase with the salinity of the raw water. Due to the fact that in the process according to the invention at least part of the first distillate is introduced into the raw water in the inflow to or in the membrane plant, the salinity of the raw water can be reduced. Due to the reduced salinity of the raw water and the pressure is lower, which is required to flow the raw water through the membrane or membranes of the membrane system. This pressure is approximately proportional to the salt concentration or to the salinity of the raw water. The lower salinity of the raw water allows, for example, cheaper membranes and pumps that withstand less pressure or have to apply less pressure to use for the membrane system.
  • the investment and operating costs for the membrane system are reduced.
  • the first brine is not discharged unused, but used for the extraction of the first distillate.
  • the first distillate in turn contributes to the production of permeate.
  • the amount of permeate produced is increased, ie the treatment ratio improved.
  • the volumetric fraction of the waste product is reduced.
  • the temperature of the raw water flowing to the membrane system can be increased. This increase in temperature can increase the efficiency with which the membrane system is operated. Both the reduction in the concentration of the component to be separated in the raw water and the heating of the raw water can lead to a cost savings in the membrane system and thus to a relatively low production in the overall system.
  • the inventors have recognized, however, that the benefits to the membrane system more than outweigh the expense of using an additional thermal system. It has been found that the overall system formed by the system according to the invention permits a more favorable production of the permeate than is possible in a single operation or in a series-connected operation of one thermal installation and one membrane installation.
  • the plant further comprises a preheater in which heat of the second brine is transferred from the thermal plant to the raw water before it enters the membrane plant. This makes it possible to increase the inlet temperature of the raw water and to advantageously change the process temperature in the membrane system, so that the membrane system can be operated more efficiently.
  • the second brine can be separated into at least a second distillate and a third brine.
  • the second distillate may be at least partially introduced into raw water, which flows to the membrane unit or is located in the membrane unit.
  • the salinity of the raw water can be further reduced and the investment and - - Drive costs of the membrane system can be further reduced.
  • the volume fraction of the residual product, namely the third brine can be further reduced.
  • Another advantage resulting from the use of the preheater is that the residue product, namely the third brine, is less warm than the second brine, thus simplifying the handling of the evacuation.
  • the process according to the invention is particularly advantageous for the treatment and processing or the concentration of raw waters which have a high concentration of a constituent to be separated, which does not or only slightly changes to the gas phase in the case of evaporation or evaporation.
  • the concentration can be reduced by introducing at least part of the first and / or second distillate.
  • the concentration of the component to be separated in the raw water in the inventive method by introducing the first and / or the second distillate by at least 5%, more preferably at least 20% and in particular reduced by at least 30%.
  • the inventive method can be used for example for the treatment of brackish water or seawater, and in particular for waters that have a salinity of> 20,000 mg / kg.
  • the unit "mg / kg" in the present specification means a concentration, and a concentration or salinity of 1 mg / kg means that 1 kg of the water added with the component contains 1 mg of the ingredient.
  • the temperature of the raw water in the inflow to or in the membrane plant with the aid of said introduction of the first and / or the second distillate or by preheating using brine from the thermal plant to a temperature of> 20 ° C, preferably of> 30 ° C and particularly preferably of> 35 ° C and / or to a temperature of ⁇ 60 ° C, preferably of ⁇ 50 ° C and particularly preferably increased by ⁇ 45 °.
  • a temperature of> 20 ° C preferably of> 30 ° C and particularly preferably of> 35 ° C and / or to a temperature of ⁇ 60 ° C, preferably of ⁇ 50 ° C and particularly preferably increased by ⁇ 45 °.
  • HT membranes high-temperature membranes
  • the preferred upper temperature limitations mentioned above do not apply.
  • the efficiency can be further increased.
  • at least a portion of the second brine is returned to a first brine, which is located in the inflow to or in the thermal system.
  • At least a part of the second brine is again subjected to the separation process of the thermal plant in at least a first distillate and a second brine, so that a concentration takes place.
  • the amount of waste product can be reduced and at the same time the yield of the first distillate can be increased.
  • the recycling in the thermal plant can be carried out for example by means of a batch operation or in a continuous operation.
  • the second brine may be supplied to the thermal process, for example, one or more additional times. Then the resulting brine can be removed and the process repeated with fresh first brine.
  • very high concentrations in the residue product and, concomitantly, an advantageously small volume of the residue product can be achieved.
  • the entire second brine is recycled.
  • the second brine can be recycled in a continuous operation of the thermal system.
  • concentration achieved is less than in the case of batch operation, but no replacement of the brine has to be carried out.
  • the second brine is recycled such that the temperature of the brine upon entry into the thermal plant ⁇ 55 ° C, more preferably ⁇ 50 ° C, in particular ⁇ 45 ° C and / or preferably> 20 ° C, particularly preferably> 30 ° C, in particular> 40 ° C. - -
  • the adjustment of the inlet temperature can be set by the recirculation time or by the amount of recirculated second brine.
  • the above-mentioned temperature ranges ensure that the upper process temperature is not exceeded.
  • the usual in the prior art methods for storing water can be used.
  • a stockpiling of the first and / or the second brine can be made.
  • the stock brine can then be reused later.
  • these known from the prior art method should not be discussed in detail in the present description.
  • Renewable energies in particular solar energy and / or waste heat or geothermal heat, can be used for the operation of the membrane installation and / or the thermal installation, for example.
  • the method according to the invention for concentration of waters, in particular of waters or tailings from the oil and gas industry, of waters from mining, of waters in electroplating or of waters in the food industry.
  • waters in particular of waters or tailings from the oil and gas industry, of waters from mining, of waters in electroplating or of waters in the food industry.
  • certain waters may be concentrated or thickened using the process of the present invention to produce sugar concentrate, concentrated juice or fruit juice concentrate.
  • the present invention further comprises a plant for the treatment of waters comprising a membrane plant and a thermal plant.
  • the membrane system is used to separate a raw water into at least one permeate and a first brine and comprises a first supply and a first and a second output.
  • Raw water is supplied to the membrane system through the first supply, and permeate or first brine is discharged from the membrane system through the first or second outlet.
  • the thermal system serves to separate the first brine into at least one first distillate and a second brine and comprises a second supply and a third and a fourth output.
  • the second feed is connected to the second output.
  • the second feed supplies at least part of the first brine to the thermal system.
  • the third or fourth outlet separates the first distillate or the second brine from the thermal plant.
  • the installation according to the invention furthermore comprises a first connection in order to supply at least a portion of the first distillate to the raw water.
  • the plant further comprises a return to at least recycle a portion of the discharged from the thermal plant second brine.
  • the discharged second brine can be supplied, for example, to the first brine in the second supply or in the thermal plant.
  • the recirculation can be outside and / or within the thermal plant.
  • the return may also include a reservoir, for example, for a batch operation in which the second brine can be subjected to the process within the thermal plant several times and in succession.
  • a reverse osmosis plant, a nanofluidization plant or an ultrafiltration plant can be used as membrane plant.
  • a thermal plant for example, a distillation plant, in particular a wet air distillation plant, a membrane distillation plant, a multi-effect distillation plant, a mechanical vapor compression system or a multi-stage flash system can be used.
  • the plant may further include a preheater to preheat the raw water for the membrane plant using second brine from the thermal plant. In this case, the second brine is at least partially transferred to a third brine.
  • the preheater includes a third supply, a fourth supply, a fifth output and a sixth output. Through the fourth supply the preheater is supplied to the preheated raw water.
  • the third supply which is connected to the fourth output of the thermal system, at least a portion of the second brine is introduced into the preheater, so that heat from the second brine can be transferred to the raw water.
  • the sixth output of the preheater which is connected to the first supply of the membrane plant, the preheated raw water is discharged. The discharged preheated raw water is fed to the membrane unit through the first supply.
  • the third brine can be removed from the preheater.
  • the second brine in the preheater can be at least partially separated into the third brine and a second distillate.
  • the preheater further comprises a seventh output and the system further comprises a second connection.
  • the second connection is connected to the first supply of the membrane unit and to the seventh output of the preheater.
  • the second distillate can be removed through the seventh outlet of the preheater and via the second connection at least partially into the raw water, which flows to the membrane unit or is located in the membrane unit, are introduced.
  • Fig. 1 is a schematic diagram of a first embodiment of the system according to the invention, with which the inventive method can be performed.
  • FIG. 2 is a schematic drawing of a second embodiment of the plant according to the invention, which further comprises a preheater for preheating the raw water.
  • the membrane system 12 includes a first supply 16, a first output 18 and a second output 20.
  • the thermal system 14 comprises a second supply 22, a third output 24 and a fourth output 26.
  • the system 10 comprises a first connection 28 between the Third output 24 and the first supply 16.
  • the system 10 includes a return 30, which connects the fourth output 26 and the second supply 22 with each other.
  • the thermal system 14 is operated by means of a heater 32.
  • the system 10 comprises a first outlet 39 and a second outlet 41.
  • the guide 39 is connected to the second outlet 20 and the second outlet 41 is connected to the third outlet 24.
  • the raw water 34 of the membrane unit 12 is supplied through the first supply 16.
  • the raw water 34 within the membrane unit 12 is separated into at least one permeate 36 and a first brine 38.
  • the permeate 36 is discharged through the first outlet 18 and the first brine 38 is discharged from the membrane unit 12 through the second outlet 20.
  • the first brine 38 is wholly or partially supplied through the second supply 22 in the thermal system 14: A portion of the first brine 38 can be removed via the first discharge 39.
  • the thermal system 14 is then the remaining non-discharged or removed part of the first brine 38 is supplied.
  • the first brine 38 is then separated into at least a first distillate 40 and a second brine 42.
  • the first distillate 40 is discharged through the third output 24 from the thermal plant 14 and fed via the first connection 28 to the raw water 34 in the inflow to the membrane unit 12. It should be noted that the distillate 40 can be supplied to the raw water 34 - unlike in FIG. 1 - also within the membrane installation 12. Furthermore, it is possible to remove part of the first distillate 40 via the second outlet 41.
  • Fig. 2 shows a second embodiment 10 'of the system according to the invention, which represents an advantageous development of the system 10 of Figure 1.
  • the system 10 'additionally comprises a preheater 44 which comprises a third supply 46 and a fourth supply 48 as well as a fifth output 50, a sixth output 52 and a seventh output 54.
  • the system 10 'contains a second connection 56 and a third outlet 58.
  • the second connection 56 connects the seventh outlet 54 of the preheater 44 with the first supply 16 to the membrane installation 12.
  • the third outlet 58 is connected via the second connection 56 connected to the seventh output 54 of the preheater 44.
  • the raw water 34 is supplied to the preheater 44 through the fourth supply 48 and the second brine 42 is supplied through the third supply 46.
  • the preheater 44 With the aid of the preheater 44, heat of the second brine 42 which has been heated in the thermal installation 14 can be at least partially transferred to the raw water 34.
  • the heated raw water 34 is discharged through the sixth outlet 52 of the preheater 44 and the membrane - - Anläge 12 supplied as preheated raw water 34 through the first supply 16. Due to the heating of the raw water 34 through the preheater 44, the membrane unit 12 can be operated more efficiently.
  • the second brine 42 in the preheater 44 is at least partially transferred to a third brine 60.
  • the third brine 60 is discharged via the fifth outlet 50 of the preheater 44 as a waste or residue product or as recovered concentrated product.
  • the preheater 44 has the function of a heat exchanger with which the heat energy of the second brine 42 can be used to increase the efficiency of the membrane system 12.
  • the discharged third brine 60 has a lower temperature than the second brine 42. This is another advantage because the handling of the discharged product is facilitated.
  • the preheater 44 thus increases the efficiency of the membrane system 12 by heating the raw water; on the other hand, it facilitates the handling of the less hot discharged third brine 60 by cooling the second brine 42.
  • the preheater 44 may be implemented as a thermal plant or as a stage of a thermal plant in which the second brine 42 is separated into the third brine 60 and a second distillate 62. This is an example of the term used above, according to which only one part of the second brine 42 is "transferred" to the third brine 60.
  • the second distillate 62 may be removed through the seventh exit 54 of the preheater 44. Subsequently, the second distillate 62 can be discharged through the third discharge 58 and / or supplied to the heated raw water 34 via the second connection 56. In this case, the second distillate 62 can be completely or partially removed from the preheater 44 or fed to the raw water 34.
  • the water production costs for a seawater reverse osmosis (MWUO) plant are much higher than the water production costs for a brackish water reverse osmosis (BWUO) plant.
  • the pressure that must be used to pump the seawater or brackish water through the membrane membrane membrane is approximately proportional to the salt concentration of the water.
  • High salt concentrations of more than 25,000 mg / kg usually require a pressure of more than 6 MPa, which must be applied by appropriate pumps.
  • With a lower salt concentration for example, brackish water with a salinity of less than 10,000 mg / kg, the pressure required is lower, so that pumps can be used, which must apply only a pressure of 1 MPa or less.
  • thermal plants the water production costs are usually higher in comparison to membrane plants.
  • the energy required to process raw water is provided by a thermal plant operating on the principle of multi-effect distillation, for example at 80 kWh / m 3 and in a thermal plant operating on the principle of wet-air distillation, for example at 200 kWh / m 3 .
  • a humid air distillation plant is indicated in which the water costs in a Capacity of 2000 m 3 / day 21.50 EUR / m 3 .
  • the plants 10 and 10 'combine the advantages of the membrane plant 12 and the thermal plant 14, namely the high throughput at low cost and the salinity-independent performance or the production of virtually salt-free distillate 40.
  • a more favorable membrane installation 12 can be used and a higher yield of permeate 36 can be achieved than would be possible without the thermal installation 14.
  • the concentration of components to be separated in the second brine 42 can be adjusted in the desired manner. Compared to the sole operation of the membrane installation 12, the second brine 42 thus also has a higher concentration than the first brine 38.
  • the scrap formed by the second brine 42 is further reduced in the system 10, since part of the second brine 42 is again used for distillate recovery, which in turn is used to reduce the salinity of the raw water 34.
  • the no longer or no longer recycled second brine 42 contains a concentrate of the components to be separated and is taken from the plant.
  • the plant 10 shown in Figure 1 is operated in continuous operation, in which the raw water 34 flows continuously and the permeate 36 and a portion of the second brine 42 flow continuously.
  • the other part of the second brine 42 is supplied via the return 30 of the first brine 38, whereby the flow of the second brine 42, which ultimately leaves the plant 10, is lower and has a higher concentration than would be the case without the return 30.
  • the thermal system 14 can also be operated in batch mode. For this purpose, for example, the entire second brine 42, which is produced within a certain time, mixed with a first brine 38 or even unmixed, one or more further times the distillation process in the thermal plant 14 are subjected. Then the brine is disposed of and the process continues with a new batch. This allows a very high concentration can be achieved, which can lead to a virtually solefree operation (Zero Liquid Discharge).

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  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Nanotechnology (AREA)
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  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

L'invention concerne un procédé et une installation (10) de traitement et de transformation d'eaux. Une eau brute (34) est amenée à un système de membranes (12) dans lequel elle est séparée en au moins un perméat (36) et une première saumure (38). La première saumure (38) est amenée dans une installation thermique (14) dans elle est séparée en au moins un premier distillat (40) et une première saumure (42). Une partie au moins du premier distillat (40) est introduite dans l'eau brute (34) qui arrive au système de membranes (12) ou qui se trouve dans le système de membranes (12).
PCT/EP2013/076465 2012-12-13 2013-12-13 Procédé et installation de traitement et transformation d'eaux WO2014090973A1 (fr)

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DE102012112215.6A DE102012112215A1 (de) 2012-12-13 2012-12-13 Verfahren und Anlage zur Aufbereitung und Verarbeitung von Wässern
DE102012112215.6 2012-12-13

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CN115367946A (zh) * 2022-09-08 2022-11-22 碧菲分离膜（大连）有限公司 一种膜蒸馏海水淡化的方法

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CN110496537A (zh) * 2018-05-18 2019-11-26 中国石油化工股份有限公司 一种太阳能热泵膜蒸馏系统
CN110510806A (zh) * 2019-08-05 2019-11-29 东莞市逸轩环保科技有限公司 电镀废水零排放处理工艺
CN111908543A (zh) * 2020-09-17 2020-11-10 成都建筑材料工业设计研究院有限公司 直接余热热源水泥生产和海水淡化联合实现系统及方法

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WO2019219472A1 (fr) * 2018-05-18 2019-11-21 Siemens Aktiengesellschaft Utilisation combinée de chaleur perdue et d'eaux usées/de saumure aux fins de la production d'eau potable dans des centrales électriques à gaz et à vapeur
CN115367946A (zh) * 2022-09-08 2022-11-22 碧菲分离膜（大连）有限公司 一种膜蒸馏海水淡化的方法

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