EP1385592A1 - Procede d'evaporation pour la production d'eau potable pure et de saumure concentree a partir d'eaux brutes salines - Google Patents

Procede d'evaporation pour la production d'eau potable pure et de saumure concentree a partir d'eaux brutes salines

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Publication number
EP1385592A1
EP1385592A1 EP01274186A EP01274186A EP1385592A1 EP 1385592 A1 EP1385592 A1 EP 1385592A1 EP 01274186 A EP01274186 A EP 01274186A EP 01274186 A EP01274186 A EP 01274186A EP 1385592 A1 EP1385592 A1 EP 1385592A1
Authority
EP
European Patent Office
Prior art keywords
evaporation
system pressure
raw water
stage
column
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP01274186A
Other languages
German (de)
English (en)
Inventor
Peter Dr.-Ing. Vinz
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Publication of EP1385592A1 publication Critical patent/EP1385592A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/26—Multiple-effect evaporating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/007—Energy recuperation; Heat pumps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
    • B01D3/343—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances the substance being a gas
    • B01D3/346—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances the substance being a gas the gas being used for removing vapours, e.g. transport gas
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy

Definitions

  • the invention relates to an evaporation process and several advantageous developments of the process for the production of sterile drinking water in distillate quality and high-percentage brine as chemical raw material from raw water with any salt content. If the evaporation process is combined with a thermal power generation process, the combination system also supplies electrical energy with '' maximum fuel utilization.
  • the method according to the invention works with a water vapor-saturated carrier gas circulation, over one or more evaporation / condensation temperature intervals arranged one above the other.
  • the carrier gas is enriched with steam in an evaporation column and in a condensation column with separation of distillate.
  • the raw water fed in serves as coolant and heats up while absorbing the heat of condensation of the condensing distillate.
  • the heat carry-over induced by the carrier gas circulation is compensated with additional thermal measures.
  • Such an evaporation process consisting of an evaporation module is described in EP 0531 293 B1.
  • two heat exchange devices of the same power are disclosed therein, through which the circulating total amount of carrier gas flows, one of which is arranged in the condensation column and the other in the evaporation column. This is intended to heat the total vapor-depleted carrier gas stream in the condensation column, absorbing the heat of liquefaction, and to transfer the absorbed heat in the evaporation column back to the evaporating medium, thus counteracting the spread of heat.
  • the main deficiency in the disclosed method lies in the heat displacement of these heat exchange devices, which is far more than compensated for in terms of performance, and in the high temperature losses due to the multiple heat transfer. Furthermore, the mechanical integration of the heat exchange devices in both pillars is complicated in construction, takes up space and is also production-intensive and costly.
  • the overcompensation of the carry-over of the carrier gas is avoided. It is based on the evaporation system disclosed and consists of an evaporation column, a condensation column, a post-heating device and a carrier gas circulation, in which the vapor-storing carrier gas is moved by a fan over an identical evaporation / condensation temperature interval in steps of temperature and quantity through and between the evaporation column and the Condensation column circulates.
  • a recuperative heat exchange device through which the raw water flows is located within the condensation column.
  • a heat exchanger formed from several cells is arranged in the problem solution according to the invention between the condensation column and the evaporation column.
  • Each of these heat exchanger cells is flowed through on the primary side by an associated vapor-saturated carrier gas transfer stream.
  • the cells are serially flowed through by salt water, which circulates through and between the heat exchanger and the evaporation column and heats from cell to cell during serial passage through the cells of the heat exchanger and reduces its amount in stages.
  • the individual quantities and temperatures of the salt water partial flows transferred from the heat exchanger to the evaporation column are those from the evaporation column equalized in terms of enthalpy to the vapor-saturated carrier gas flows transferred to the condensation column.
  • the reheated partial salt water streams are introduced into the evaporation column at approximately the same temperature feed points and thus counteract the carry-over of heat from the carrier gas circulation. As they pass through the evaporation column, they evaporate together with the main salt water stream while cooling.
  • the total amount of circulating salt water to be supplied to the heat exchanger is replenished either from the concentrate outlet or from the raw water inlet.
  • the heat exchange capacity to be installed for the compensation of the heat carry-over is reduced from 2 x 210 kW to less than 70 kW i.e. for a distillate capacity of 1000 kg / h water. to 1/6 of the previous heat transfer capacity. The temperature losses decrease by half.
  • the different heat exchange performances which serve the same purpose result from the physical fact that with a fixed total system pressure for storing equal amounts of steam in the carrier gas a larger amount of gas is required for storing with a low partial vapor pressure than for storing the same amount of steam with a high partial vapor pressure. For this reason, the carrier gas quantities to be transferred from the evaporation column to the condensation column decrease exponentially with increasing saturation temperature over the working temperature interval of the columns.
  • the carrier gas partial quantities cumulative to the circulating total quantity must therefore not, as disclosed in the document, pass through the entire working temperature interval of the columns as a whole, but the largest carrier gas partial quantity only the smallest temperature interval and the smallest carrier gas partial quantity the entire temperature interval.
  • the amount of carrier gas to be transferred is zero.
  • the concentrate outlet can be concentrated in a particularly advantageous manner up to close to the precipitation concentration. This is particularly useful with limited salt water reserves or for the production of concentrated brine as a chemical raw material from the unlimited available sea water.
  • the amount of salt water circulating between the multi-cell heat exchanger and the evaporation column not only compensates for the carry-over of heat from the carrier gas circulation, but it also gradually replaces the amount of salt water reduced by evaporation within the evaporation column and compensates for changes in enthalpy of the evaporation salt water.
  • the specific evaporation quantity in the evaporation column increases with decreasing evaporation temperature, whereas it would decrease without this salt water circulation. This results in a lower specific post-heating requirement for distillate extraction.
  • Another embodiment of the method according to the invention is that the multi-cell heat exchanger is combined with the recuperation device arranged in the condensation column or integrated in the column and the heat exchange surface of the recuperation device is increased in zones by the power values of the individual heat transfer cells of the external heat exchanger and that from the Recuperation device with tiered and temperature-adjusted raw water partial quantities are drawn off and led to the same temperature locations in the evaporation column.
  • the columns can be manufactured as evaporation modules, in a space-saving and cost-saving coaxial design, with a pressure-stable outer jacket. This noticeably reduces the effort for pipelines, valves and pressure vessels as well as for the pipeline connections and the consumption of expensive seawater-resistant materials is reduced to a minimum.
  • evaporation modules can be connected in groups of any number in parallel and in series in up to 4 system pressure levels to increase the capacity of drinking water production.
  • a system pressure gradation reduces the amount of carrier gas circulating in the lower system pressure levels and thus their heat transfer.
  • this allows the evaporation temperature interval to be extended to 220 K and the system pressure level arranged below to be heated with the waste heat from a higher system pressure level. This in turn reduces the external cooling capacity in the lowest system pressure level.
  • the specific thermal energy consumption for the production of drinking water from raw water regardless of its salinity, can be reduced to values below 10 kWh / m 3 .
  • the modular design also allows the production of larger and thus more cost-effective production lots in largely automated production plants.
  • the system pressure levels of the evaporation modules are preferably determined in such a way that the same evaporation vapor temperature differences are processed in the series-connected modules with matched specific evaporation rates, which build on one another and thus extend the total evaporation temperature interval of the evaporation system.
  • the total system pressures in the evaporation modules are determined via the carrier gas fill quantities, whereby the operating values in the individual system pressure stages only when the above the evaporation temperature determined by the external heating source. Ambient air is preferred as the carrier gas for evaporation plants for drinking water production.
  • a mechanical filter device with which suspended matter is removed from the raw water is associated with an evaporation system on the raw water supply side.
  • Salt water from the concentrate outlet or a second quantity of raw water used as a coolant for the evaporation plant can advantageously be used for the automatic backwashing.
  • the operating pressure levels of the evaporation modules can be set to the optimal collector operating conditions.
  • the waste heat from electricity-producing gas turbines or internal combustion engines is particularly suitable.
  • the evaporation modules connected in parallel and in series can outnumber them Temperature level and the amount of waste heat available.
  • the electricity-producing part of such a system supplies the own electricity consumption for the entire system and feeds excess electricity, for example, into a public supply network. Up to 85% of the fuel can be used in such systems.
  • reverse osmosis and / or electrodialysis systems can also be connected upstream or in parallel to these systems on the raw water supply side.
  • it only makes sense to switch it on if the specific energy consumption taking into account the conversion losses is not higher than that of the evaporation plants themselves.
  • the salt concentration of the raw water to be fed changes periodically, for example due to the tidal effect at which Extraction of raw water from estuaries.
  • the distillate obtained with such an evaporation plant can be blended for drinking water treatment with a portion of the pre-cleaned raw water and / or with the permeates of the mechanical or electrical processes. These portions pass through a UV irradiation device for sterilization and are then mixed into the distillate.
  • FIGS. 1 to 5 The invention is described in more detail with reference to FIGS. 1 to 5.
  • the figures show in detail:
  • FIG. 1 the process diagram of a single-stage evaporation module with a heat exchanger arranged outside the columns to compensate for the heat carryover of the carrier gas circulation
  • FIG. 2 the process diagram of an evaporation system consisting of three system pressure stages, each with an evaporation module in the system pressure stages and with the systems combined with the recuperation devices for compensating the heat carry-over,
  • FIG. 3 the procedural block diagram of an evaporation plant heated with waste heat from the generation of power for producing drinking water and electrical current
  • FIG. 4 the process engineering diagram of an evaporation plant for the production of drinking water and high-percentage brine
  • Figure 5 an alternative block diagram of an evaporation plant for the production of drinking water and high-proof brine with optimized energy consumption values.
  • the evaporation module shown schematically in Figure 1 consists of the evaporation column (1), the condensation column (2), the multi-cell heat exchanger (3) and the post-heating device (4). Between and through the columns (1) and (2) the vapor-storing carrier gas (6), in the special case air, moved by a fan (5) circulates.
  • the recuperative heat exchange device (7) is arranged in the condensation column (2).
  • the pump (8) conveys the raw water (9) for recuperative heating through the heat exchange device (7).
  • the recuperatively heated raw water (9) is passed through the post-heating device (4), heated to the upper evaporation temperature and then introduced into the evaporation column (1) at the top (10).
  • the evaporation column (1) contains superimposed heat and mass transfer packs (11.01 to 11.15) which are flowed through vertically from top to bottom by the heated raw water (9), which evaporates into the opposite air flow (6) on the way down cools. Clearances (12.1 to 12.15) are formed between the packs (11.01 to 11.15).
  • the cold concentrate (13) is removed by the pump (14) at the bottom (15) of the evaporation column (1).
  • the partial flow (16) for example of the concentrate drain (13), is fed to the heat exchanger (3) as a total. When heated, it flows through the cells on the secondary side (3.01 to 3.15). In each case between two cells, a partially heated partial flow (16.01 to 16.15) of the circulating salt water (16) is returned from the heat exchanger (3) to the evaporation column (1).
  • the heated last partial stream (16.15) is combined with the recuperatively heated raw water (9) and fed to the post-heating device (4).
  • the transferred salt water partial flows (16.x) and the transferred steam-saturated air flows (6.x), each with the same atomic number (x), are equalized in the enthalpy amount.
  • the distillate (17) is derived with the pump (18) on the bottom (19) from the condensation column (2) of the evaporation module and used.
  • the number of partial flow transfers in an evaporation module depends on the total system pressure and the temperature interval that is processed in the columns.
  • the multi-stage evaporation system shown schematically in FIG. 2 consists of the pressure-stage evaporation modules (A, B, C). Each evaporation module contains an evaporation column (A-1, B-1, C-1) and a condensation column (A-2, B-2, C-2). In the condensation columns (A-2, B-2, C-2) there are the associated recuperative heat exchange devices (A-3, B-3, C-3) for preheating the raw water together.
  • the steam-saturated air flow (A-5) moved by the fan (A-4) circulates.
  • the saturated air flows (B-5) and (C-5) circulate in the same way as in module (A).
  • the operating pressures in the evaporation modules (A, B, C) are adapted to the individual, complementary evaporation temperature intervals.
  • the raw water (20) is conveyed serially by the pump (21) through the recuperation devices (A-3, B-3, C-3) and heated up to the final recuperative temperature.
  • the heated raw water (20) is then passed through the post-heating device (22), heated to the upper evaporation temperature in the latter and then introduced at the top (C-9) into the evaporation column (C-1).
  • the raw water (20) flows through the heat and mass transfer packs (C-10).
  • the partially evaporated raw water (C-23) is discharged from the evaporation column (C-1), expanded in a throttle valve to the pressure of the evaporation module (B) and at the head ( B-9) introduced into the column (Bl).
  • the partially evaporated raw water (C-23) flows through the columns (Bl) and (Al) one after the other with a stepped system pressure reduction and further evaporation and cooling in the same way as the column (C-1).
  • the final concentrate (A-23) is removed with the pump (A-24) from the atmospheric evaporation module (A) and sent for disposal.
  • recuperative heat exchange devices From the recuperative heat exchange devices (A-3, B-3, C-3), as shown and described in FIG. 1 for the multi-cell heat exchanger (3), the individual from the evaporation columns (Al, Bl, C-1) the condensation columns (A-2, B-2, C-2) transferred vapor-saturated partial air flows (A-5x, B-5x, C-5x) enthalpy-adjusted raw water partial flows (A-20x, B-20x, C-20x) and these at same temperatures at the corresponding locations in the evaporation columns (Al, Bl, C-1).
  • the salt water (A-25, B-25, C-25) circulating between the heat exchange devices (A-3, B-3, C-3) and the evaporation columns (Al, Bl, C-1) is used for each evaporation stage (A , B, C) separately with the pumps (A-24, B-24, C-24) from the respective concentrate drains (A-23, B-23, C-23) the raw water (20) at the appropriate place, before entry fed into the recuperative heat exchange devices (A-3, B-3, C-3).
  • the distillate portion (CB-26) is expanded to the system pressure level of the condensation column (A-2) and into the head (A-28) initiated.
  • the distillate portion (CB-26) combines with the distillate portion (A-26) which condenses out of the steam-saturated air circulation (A-5) and cools with it on the flow path from top to bottom in the condensation column (A-2).
  • the distillate (ABC-26) collecting on the bottom (A-27) is sucked out of the condensation column (A-2) by the pump (29) and used.
  • FIG. 3 shows a complete thermal system based on the evaporation principle for the production of drinking water from salt water in its most favorable embodiment as a unit supplying electricity and drinking water.
  • the evaporation modules are only shown in a simplified form.
  • possible plant expansions to increase drinking water production using excess electricity are shown in dashed lines.
  • the system concept is based on the use of waste heat from an electricity-producing gas turbine (30), the generator (31) of which is the self-consumption of the evaporation plants (32) and the upstream and parallel electricity consumers EDS (33), ED (34), RO (35) and the feed pumps ( 36, 45, 47) and the UVS sterilization device (37) are supplied with current. Excess electricity is fed into a supply network.
  • the multi-stage evaporation plant (32) is supplied with the exhaust gas heat of the gas turbine (30) via the exhaust gas heat exchanger (38) for reheating the recuperatively heated raw water (41).
  • the unpurified raw water (39) is conveyed by the pump (36) for the removal of suspended matter through the filter unit (40) and then in the selectively cleaning electrodialysis device (33) in countercurrent to the coolant drain (46) of the evaporation plant from the crust-forming, dissolved Salt free.
  • the pre-cleaned raw water (41) passes under heating tion and re-liquefaction of the water vapor, the recuperation devices arranged in the condensation part of the system and is heated in the exhaust gas heat exchanger (38) with the turbine waste heat to the upper evaporation temperature and then introduced into the evaporation part of the system.
  • the distillate (42) is removed from the condensation part of the plant.
  • the brine pump (48) disposes of the concentrated brine (45) from the evaporation part.
  • the cooling water pump (47) conveys the cooling water (46) through the coolers of the evaporation plants and through the secondary side of the electrodialysis system (33).
  • the cooling water is also used for filter backwashing and then disposed of.
  • the tasks of the cooling water can also be performed by the concentrate drain of an upstream or parallel RO system.
  • the distillate (42) is blended with the partial flow (43) of the pre-cleaned raw water (41) to drinking water (44) and then used.
  • the pre-cleaned raw water partial stream (43) used as blended water is passed through the UVS sterilization device (37) before the mixing process for sterilization and then mixed with the distillate (42).
  • FIG. 4 shows the process flow diagram for the combined production of drinking water in distillate quality and high-percentage brine as chemical raw material. Both products are obtained from raw water with any initial salt content.
  • Up to 9 evaporation systems (I, II, ... IX) consisting of three system pressure levels (D, E, F) in the case shown are separated from the raw water to be treated (100) between the raw water inlet (101) and the brine outlet (102). flowed through under constant evaporation.
  • Each system pressure stage (D, E, F) represents one of the 27 evaporation stages (1, ... 27).
  • Each evaporation stage (1, ... 27) can in turn consist of several (not shown) evaporation modules through which raw water flows in parallel according to Fig 1 or 2 exist.
  • the total number of evaporation stages (1, .. 27) results from the initial and final concentrations of the salt water and from the specific evaporation rates possible within the temperature intervals of the individual evaporation stages (1, ... 27).
  • the number of evaporation stages (1, ... 27) can range between 10 for single-stage, atmospheric systems and 30 for systems with 3 to 4 system pressure levels (D, E, F).
  • the total number of evaporation modules is independent of the number of system pressure levels (D, E, F), it is determined by the drinking water yield. The number of modules is greatest in the first evaporation stage and smallest in the last evaporation stage. In accordance with the distillate yield, it decreases as an integer from stage to stage.
  • the raw water (100) to be fed is conveyed by the raw water pump (103) in adapted amounts through the first evaporation system (I).
  • the raw water main stream (104) flows under heating by absorption of the liquefaction heat of the distillate obtained, the recuperation device (F-105), is recombined with the portion (106) branched off for the distillate cooling of the middle system pressure stage (E) and flows through together with it Heating by absorption of the liquefaction heat of the resulting distillate, the recuperation device (E-105), is combined with the partial amount (107) branched off for the distillate cooling of the upper system pressure stage (D) and flows through the recuperation device together with this under heating by absorption of the liquefaction heat of the resulting distillate (D-105).
  • the raw water total flow in the heat exchanger (108) is heated with external energy to the upper evaporation temperature of the upper system pressure stage (D) and then into the (not shown) evaporation device according to FIG. 1 or Fig. 2 of this system pressure stage (D) initiated.
  • the partially concentrated salt water flowing out of the first evaporation system (I) without pressure is conducted with the pump (110) through the externally cooled heat exchanger (111), pre-cooled therein with a second raw water stream (112) and in the same way through the second evaporation system (II ) and recuperatively heated, as described in detail for the raw water fed into the first evaporation system (I).
  • the distillate of the higher system pressure levels (D, E) is collected from the evaporation system to the evaporation system and heats in separate distillate coolers (D-113, E-113) the salt water partial quantities (106, 107) branched off from the raw water main stream (101) as required upper evaporation temperature of the system pressure level (E, F) below.
  • the branched-off partial streams (106, 107) become part of their heating again the raw water main stream (104) merged. This means that the system pressure levels (D, E, F) and also the same system pressure levels of the subsequent evaporation systems (II to IX) always have balanced quantity and heat ratios.
  • Distillate pumps (D-114, (E114), (F114) assigned to the system pressure stages (D, E, F) convey the distillate from the evaporation systems into a distillate pressure accumulator (115) .
  • the cooling water pump (116) conveys raw water (117) as coolant through the Cooler (111)
  • the concentrated brine (102) is fed with a feed pump (118) from the last evaporation stage (27) for further processing.
  • Figure 5 shows the block diagram of an energetically optimized system for the production of drinking water and high-percentage brine with the least amount of pump energy.
  • up to 18 evaporation stages are arranged at two system pressure levels (G, H), of which the first nine evaporation stages work in the upper (G) and the second nine in the lower system pressure stage (H).
  • the raw water to be treated (150) is conveyed with the raw water pump (151) into the upper system pressure stage (G).
  • the majority of the raw water (152) passes through the recuperation device of the tenth evaporation stage (10) while being heated.
  • An adapted portion of raw water (154) passes the distillate cooler (155) and is heated in countercurrent from the amount of distillate (156) collected in the upper system pressure stage (G) to the upper evaporation temperature of the lower system pressure stage (H).
  • both preheated raw water partial flows (152, 154) are combined and the total amount (150) is passed through the recuperation device (157) of the first evaporation stage (1) in the upper system pressure stage (G) while being heated.
  • the raw water (150) is reheated to the upper evaporation temperature of this evaporation stage (1) by means of the heating device (158) and then introduced into the evaporation device (not shown) according to FIG. 1. It flows through the evaporation device with evaporation and cooling.
  • the pump (160) conveys the partially concentrated salt water outlet (159) from the first evaporation stage (1) for pre-cooling and stabilization of the lower evaporation temperature in the pressure-equal, second evaporation stage (2) through the heat exchanger (161).
  • the salt water (159) passes under heating, the recuperation device (162) and the outer heating device (163) of the second evaporation stage (2) and is introduced with the upper evaporation temperature into the evaporation device (not shown) according to FIG. 1 of this evaporation stage (2) ,
  • the salt water drains of the subsequent, likewise pressure-equal evaporation stages (3) to (8) are conveyed in the same way from evaporation stage to evaporation stage through the upper system pressure stage (G) and the salt water outlets are each subjected to the heat treatment described.
  • the salt water outlet (164) of the ninth evaporation stage (9) is expanded in a throttle valve (165) to the system pressure of the lower system pressure stage (H) and introduced into the tenth evaporation stage (10) without reheating.
  • the pump (166) conveys the salt water outlet (167) of the tenth evaporation stage (10) through the cooler (168).
  • the salt water (167) passes through the recuperation device (169) of the same pressure, eleventh evaporation stage (11) and the heat exchanger (161) while heating. With the upper evaporation temperature of the lower system pressure stage (H), the salt water (167) is introduced into the evaporation device (not shown) of the eleventh evaporation stage (11). With further pumps (166) the following, pressure-equal salt water processes promoted from evaporation stage to evaporation stage and the salt water drains exposed to the heat treatment described. The highly concentrated brine (170) is fed for further processing by the brine pump (171). The distillate drains (152, 172) of the two system pressure stages (G, H) are pumped (173, 174) into the distillate pressure vessel (175). The cooling water pump (176) supplies the coolers (168) arranged in the lower system pressure stage (H) with a second stream of raw water (177) which is disposed of after it has been heated.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

L'invention concerne un procédé économique et des dispositifs pour extraire de l'eau potable de qualité distillée et de la saumure concentrée, sous forme de matière première chimique, à partir d'eaux brutes présentant des teneurs en sel quelconques. Associés à un processus de production d'énergie thermique, ces dispositifs fournissent en outre du courant avec un taux d'exploitation du combustible supérieur à 85 %. Ce procédé d'évaporation utilisant la chaleur perdue fonctionne avec une circulation d'air saturé en vapeur d'eau, sur un intervalle de température, les eaux brutes étant soumises à un préchauffage à récupération. Ces dispositifs peuvent être constitués d'un grand nombre de modules d'évaporation et par conséquent être adaptés à chaque besoin en eau potable. Les modules d'évaporation fonctionnent avec jusqu'à 4 étages de pression de système et peuvent utiliser la chaleur perdue des étages de pression de système supérieurs dans les étages de pression de système situés en aval. Ces dispositifs permettent d'obtenir des valeurs de consommation de chaleur inférieures à 10 kWh/m<3> d'eau potable. La conception modulaire permet de couvrir une plage de débits allant de 3,0 à 1000 m<3>/h d'eau potable au moyen de turbines à gaz/d'ensembles générateurs courants. On peut obtenir des débits d'eau potable inférieurs en exploitant la chaleur perdue de moteurs à combustion interne.
EP01274186A 2001-05-02 2001-10-26 Procede d'evaporation pour la production d'eau potable pure et de saumure concentree a partir d'eaux brutes salines Withdrawn EP1385592A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE10121374 2001-05-02
DE10121374 2001-05-02
PCT/DE2001/004072 WO2002087722A1 (fr) 2001-05-02 2001-10-26 Procede d'evaporation pour la production d'eau potable pure et de saumure concentree a partir d'eaux brutes salines

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EP1385592A1 true EP1385592A1 (fr) 2004-02-04

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EP01274186A Withdrawn EP1385592A1 (fr) 2001-05-02 2001-10-26 Procede d'evaporation pour la production d'eau potable pure et de saumure concentree a partir d'eaux brutes salines

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MA26112A1 (fr) 2004-04-01
TNSN02047A1 (en) 2004-03-05
US20020166758A1 (en) 2002-11-14
CN1522168A (zh) 2004-08-18
WO2002087722A1 (fr) 2002-11-07

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