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WO2014195110A1 - Installation et procédé de traitement d'eau - Google Patents

Installation et procédé de traitement d'eau Download PDF

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Publication number
WO2014195110A1
WO2014195110A1 PCT/EP2014/060040 EP2014060040W WO2014195110A1 WO 2014195110 A1 WO2014195110 A1 WO 2014195110A1 EP 2014060040 W EP2014060040 W EP 2014060040W WO 2014195110 A1 WO2014195110 A1 WO 2014195110A1
Authority
WO
WIPO (PCT)
Prior art keywords
water
evaporator
condenser
heat exchanger
pressure
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.)
Ceased
Application number
PCT/EP2014/060040
Other languages
German (de)
English (en)
Inventor
Vladimir Danov
Thomas Hammer
Jochen SCHÄFER
Martin Tackenberg
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.)
Siemens AG
Siemens Corp
Original Assignee
Siemens AG
Siemens Corp
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 Siemens AG, Siemens Corp filed Critical Siemens AG
Publication of WO2014195110A1 publication Critical patent/WO2014195110A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/28—Evaporating with vapour compression
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/14—Evaporating with heated gases or vapours or liquids in contact with the liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/16—Evaporating by spraying
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0033—Other features
    • B01D5/0039—Recuperation of heat, e.g. use of heat pump(s), compression
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B01D5/006—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation
    • 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
    • C02F1/10—Treatment of water, waste water, or sewage by heating by distillation or evaporation by direct contact with a particulate solid or with a fluid, as a heat transfer medium
    • C02F1/12—Spray evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/32—Hydrocarbons, e.g. oil

Definitions

  • the invention relates to a plant for treating What ⁇ ser, which is obtained in the promotion of a fossil fuel, has contains impurities and geothermal energy.
  • the plant comprises at least one separating device for separating contaminants from product water to be recovered from the water.
  • the invention relates to a method for treating water.
  • Plants are known from the prior art in which the separation of a mixture consisting of petroleum, gas, water and solids, ie the treatment of the resulting in the production of fossil fuels water via two sequentially arranged separators.
  • the Separa ⁇ tors can differentiate here in terms of the prevailing pressure and the present temperature. Usually the majority of the water is separated in a high-pressure separator at a pressure of 50 bar. In subsequent sequent ⁇ low pressure separator nearly the entire remaining 2% of the water present in the mixture to be separated bar at around 10 degrees.
  • the separated water usually contains more residual oil, salts, and smaller amounts solids in concentra ⁇ tions, which do not allow for environmentally friendly disposal. Even for a direct reuse of this water, the quality is usually not enough.
  • Aurusi ⁇ processing of this water for instance for further use in oil production, therefore consuming, multi-step separation method are used, which lent the separation of remaining solids and fine oil droplets as well enable desalting.
  • me ⁇ chanic filter method for the separation of solids an electrostatic oil separation and as a final step for desalination the reverse osmosis are used.
  • the liquid supplied to the evaporators is heated in a heat exchanger, to which a heated in a device heat transfer fluid is supplied.
  • the cooled heat transfer fluid is used in the - also successively flowed through - capacitors as a cooling medium for the carrier gas.
  • Object of the present invention is therefore to provide a system of the type mentioned above and a method for treating water, which or which allows recovery of product water in a particularly favorable manner.
  • the at least one separating device comprises at least one evaporator and at least one capacitor.
  • the impurities having water can be performed in a circuit.
  • the ⁇ we tendonss a separation means is at least one heat exchangers associated shear, in which the geothermal energy containing water is introduced as a heating medium.
  • Using the at least one heat exchanger is at least a portion of the geothermal energy to the at least one encryption dunster suppliable and the impurities having What ⁇ ser transferable.
  • the polluted water produced by the extraction of fossil fuel usually has a high heat content.
  • the geothermally induced specific heat content of the contaminated water is also particularly high.
  • This heat content can be used in the evaporator to heat a gaseous medium introduced into the evaporator.
  • the heated gaseous medium can then absorb a particularly large amount of water vapor, which can be separated after the subsequent condensation process in the at least one condenser as product water.
  • the waste heat of the contaminated water itself is thus used as a heat source for the evaporation process.
  • the at least one heat exchanger transmits geothermal energy to the contaminated water before it enters the at least one evaporator. It can be dispensed with an external heating energy source. This makes the system particularly energy-efficient and enables the extraction of product water in a particularly favorable manner. Also may be subjected to at least one evaporation and Rekondensationszyklus un ⁇ so virtually all of the contaminated water. Thus, it is possible to recover almost 100% of the water content contained in the contaminated water as product water. This clean product water or process water can then, for example, again for the
  • the at least one evaporator has a first inlet for the contaminated water.
  • a gaseous medium can be introduced via a second inlet of the evaporator, which is designed to receive water vapor originating from the contaminated water.
  • the Verdunster preferably has at least one outlet through which the water vapor laden with the gaseous ⁇ Me dium can be discharged from the Verdunster.
  • the loaded medium can be introduced into the at least one condenser, which serves to transfer the water vapor contained in the gaseous medium into the product water. As can be readily separated from the contaminated water, the product ⁇ water.
  • gaseous medium for receiving the water vapor originating from the contaminated water in particular a gas or gas mixture is suitable, which behaves inertly in the working area of the plant characterized by a temperature interval and by a pressure interval, i. in particular, neither appreciably chemically reacted nor condensed.
  • the gaseous medium which receives in the at least one Ver ⁇ darkest water vapor, transported to the at least one condenser and emits there by condensation, ambient air can include or be. It comes beispielswei ⁇ se ambient air for use as this is cost effective to Ver ⁇ addition. Ambient air can be saturated well with the water vapor originating from the contaminated water. In addition, from the enriched with water vapor ambient air in the at least one condenser, the water vapor can be converted by condensation into the product water well.
  • the gaseous medium which receives in the at least one Ver ⁇ dunster water vapor, transported to the at least one capacitor and there emits by condensation may also include or be an inert gas.
  • an inert gas such as nitrogen is possible as gasförmi ⁇ ges medium for receiving the water vapor.
  • the contaminated water or mixture which the at least one Evaporator is supplied namely usually contains gas with combustible components.
  • the inert gas When the inert gas is used as the gaseous medium used, are preferably devices for gas-tight Verschlie ⁇ SEN of the plant and / or for evacuating the installation and / or for the storage or generation of the inert gas and / or for introducing the inert gas into the at least one Trenneinrich ⁇ provided for. This serves the process-safe handling of the inert gas.
  • the first inlet for the contaminated water and the second inlet for the gaseous medium are arranged on the at least one evaporator such that the water and the gaseous medium flow through the evaporator in countercurrent. Then, a good transition of the water vapor from the contaminated water is allowed in the medium.
  • a convective-driven or convective-supported evaporation of the water is well feasible.
  • the water can be supplied via the first inlet in particular a Verrieselungs worn or the like water distributor, over which can be wetted by the medium umströmbare arranged in the evaporator structures with the contaminated water.
  • a particularly good distribution of the contaminated water can be ensured in the evaporator.
  • the at least one evaporator has a further outlet, which is coupled via a connecting line with the at least one capacitor. Via the connecting line, by the gaseous medium from the cooled water to a minimum ⁇ Verdunster the at least one capacitor fed, wherein the cooled water is used to liquefy the water vapor.
  • this cooled residual water ei ⁇ ner further use can be supplied, namely a use as a cooling medium for liquefying the water vapor. This is particularly favorable from the point of view of the process.
  • the system has a supply line through which the water used for liquefying the water vapor in the at least one capacitor ⁇ set in the at least one evaporator is traceable.
  • the water used for liquefying the water vapor in the at least one capacitor ⁇ set in the at least one evaporator is traceable.
  • the feed conduit to a junction Steep over which the capacitor from the one coming water is introduced the impurities having to and ⁇ least a Verdunster water to be supplied into the at least.
  • the impurities having to and ⁇ least a Verdunster water to be supplied into the at least.
  • the mixing brings about an increase in the temperature of the water supplied to the evaporator, if the contaminated water is warmer than the water coming from the condenser. By this mixing, a direct heat transfer can be realized without the need for another heat exchanger needs to be provided.
  • a high heat content of the water supplied to the Verdunster is advantageous.
  • Such a high heat content can be achieved in particular by the admixing of comparatively hot, impurities exhibiting water in the water coming from the condenser.
  • the contaminated water having temperatures of less than 100 ° Celsius
  • the water can be supplied to the Ver ⁇ dunster directly.
  • Such a design of the system is particularly simple. However, if the temperature is significantly less than 100 ° Celsius, so the encryption can be connected upstream dunster a heater so mög ⁇ lichst much product water from the contaminated water can be recovered.
  • the supply ⁇ line over which the evaporator with the condensate from the coming contaminated water is acted upon is passed through the at least one heat exchanger. Then, by means of the heat exchanger, the temperature of the contaminated water is lowered to an uncritical value, namely to a value below the boiling point at the working pressure of the plant. At the same time, the water coming from the condenser is heated up by the heat transfer taking place in the heat exchanger. The then high heat content of the supplied via the supply line to the evaporator contaminated water allows a particularly high recovery rate, ie the recovery of a particularly large amount of product water.
  • the system comprises at least two separating devices with a respective evaporator and a respective condenser, wherein the evaporators and the condensers are each arranged to flow through the system in succession.
  • a respective cooling device may be arranged upstream of the respective capacitors of the at least two separation devices. Such pre-cooling - or arranged in between two capacitors cooling device intercooling - ensures particularly is nearly independent of the transfer of the water vapor in the liquid Artswas ⁇ ser.
  • At least one pressure reducer upstream of an inlet of the water having the impurities into the at least one evaporator by means of which the pressure of the water to be introduced into the at least one evaporator can be reduced.
  • the pressure reduction takes place in an advantageous manner after cooling the water to be supplied to temperatures below the boiling point in the system. This makes the system particularly robust and reliable, as suddenly occurring boiling processes are avoided.
  • the at least one pressure reducer is designed as a device for obtaining mechanical and / or electrical energy.
  • a pressure regulating valve as pressure Minde ⁇ rer
  • a turbine which provides mechanical energy.
  • This mechanical energy can be used, for example, for driving pumps or blowers, which can be used for conveying the water and / or the medium.
  • the mechanical energy can also be converted into electrical energy and thus the electrical energy in the plant itself or otherwise used. This also contributes to the particularly high energy efficiency of the system.
  • the on ⁇ location comprises at least one upstream of the at least one Ver ⁇ dunsters arranged filter means for pre-cleaning of the impurities comprising water.
  • the contaminated water can be handled particularly well in the system.
  • the water having the contaminants located on the output side of such a filter device, the water having the contaminants usually having a comparatively high pressure and a relatively high temperature before, so that its heat ⁇ energy for the evaporation process in the one we can Verdunster ⁇ iquess be used particularly well.
  • a filter device in particular a Hoch horrinpara ⁇ tor can be used, which allows a separation of a large part of the water from the funded, fossil fuels, water and solids containing and geothermally heated mixture.
  • impurities are separated from the water by means of at least one separating device.
  • product ⁇ water is obtained.
  • the water having the impurities is circulated in the at least one separating device via at least one evaporator and at least one condenser.
  • the at least one separation device is associated with a heat exchanger at least, in which the water-containing geothermal energy is placed as the heating medium a ⁇ .
  • the at least one heat exchanger At least a portion of the geothermal energy is transferred to the water supplied to the at least one evaporator and containing the contaminants.
  • the at least one evaporator and / or the at least one condenser are operated at a temperature which is lower than the boiling point of water at the pressure prevailing in the at least one evaporator and / or in the at least one condenser.
  • the po ⁇ tentielle energy of the resulting high-pressure water in the system for the operation of gaseous or liquid media promoting auxiliary equipment is used. This brings a high energy efficiency of the system with it.
  • FIG. 1 a further variant of the system according to FIG 1, in which as a pressure reducer a turbine comes to Einsat; and schematically another variant of the system, in which the treatment of the water follows in several stages.
  • a system 1 shown schematically in FIG 1 is used for stor ⁇ ride of water which is obtained in the oil and gas production.
  • a mixture is conveyed which comprises oil, gas, a generally increasing depth of water and solids.
  • this contaminated water has a geothermally increasing specific heat content with increasing depth.
  • for conveying oil or gas from a source layers which runs out, pressed into the water ⁇ se layers and then correspondingly promoted a mixture which holds a further increased amount of water ⁇ ent.
  • Such a geothermally heated mixture from a deep or depleted source is fed via a feed line 2 to a filter device in the form of a separator 3 of the system 1.
  • the separator 3 is presently designed as a high-pressure separator and is preferably operated at a pressure of about 50 bar be. About the separator 3 can already be separated bring a large part of the pressed-in water in the ground from the mixture. However, this also contains this separated water nor impurities in the form of oil residues, salts, solids and the like.
  • this contaminated water is fed in Appendix 1 to a further treatment.
  • the geothermal energy of the subsidized mixture is used. This is even more meaningful because the pumped from great depths mixture usually holds geothermal energy to a considerable extent ent ⁇ .
  • the contaminated water coming from the separator 3 is fed to a heat exchanger 5 via a line 4.
  • this wastewater of the separator 3 releases heat, and moreover, due to the pressure loss occurring in the heat exchanger 5, the water is released.
  • valve 6, which is present example as a three-way valve Darge ⁇ represents, the cooled water in the heat exchanger 5 via a further line 7 a pressure reducer 8 is supplied.
  • the further relaxed at the pressure reducer 8 water is introduced at a junction 9 in a feed line 10, which leads from a condenser 11 of the system 1 to a evaporator 12 of the system 1.
  • the evaporator 12 and the condenser 11 are components of a thermal separator of the system 1. In the evaporator 12 as well as in the condenser 11 prevails in the present case preferably atmospheric pressure.
  • the supply line 10 is passed through the heat exchanger 5.
  • the heat exchanger 5 therefore, the contaminated water is cooled and at the same time the water coming from the condenser 11 is heated.
  • the evaporator 12 has an inlet 13, from which the water heated in the heat exchanger 5 passes to a water distributor 14, which is arranged in the evaporator 12.
  • evaporator 12 structures 15 which may be formed as a grid, for example, sprinkled with the heated water.
  • air is introduced into the evaporator 12, which is colder than the water introduced via the inlet 13. This air flows through the evaporator 12 in countercurrent to the emerging from the water manifold 14 water, ie in the direction opposite to the water.
  • the air is heated up and part of the polluted water evaporates into the opposite flowing, heating air. By heating the air, this is able to absorb more water vapor.
  • the air enriched with the water vapor is then fed via a Lei ⁇ tion 17, which is connected via a further outlet 44 of the evaporator 12 to the evaporator 12, the condenser 11, which is colder than the evaporator 12. Condensed in the condenser 11 then much of the water vapor.
  • Product water obtained by liquefying or condensing the water vapor is removed from the condenser 11 of the system 1 via a line 18.
  • the residual water not converted into water vapor is used in the present case, which is withdrawn from the evaporator 12 via a water outlet 19.
  • This residual ⁇ water as exemplified herein, via another valve 20, which may be formed, for example, as a three-way valve, get into a connecting line 21 through which the evaporator 12 is fluidically connected to the capacitor 11.
  • connection line 21 a pump 22 and an (optional) cooler 23 are presently arranged.
  • the radiator 23 the temperature of the water flowing through the connecting line 21 to the condenser 11, used as a cooling medium water can be further reduced. Consequently, the water vapor can be converted into liquid water in the condenser 11 particularly well.
  • the cooler 23 can be acted upon via a further line 24 with a cooling medium, for example with cooling water.
  • a partial flow can be branched off from the water leaving the evaporator 12, which partial flow is contaminated comparatively strongly with concentrated impurities.
  • This branching of water to be disposed of can take place via a further line 25.
  • For energizing the vaporizer 12 with the air blower is vorlie ⁇ quietly 26 is provided, which is arranged in a capacitor 11 connected with the Verdunster 12 Zu Kunststoff Consumer 27th Via the line 17 and the supply air 27 so the used for receiving the water vapor in the evaporator 12 air in the separator is recycled.
  • the water introduced via the connecting line 21 to the condenser 11 for cooling the water vapor water leaves the Kon ⁇ capacitor 11 again via the supply line 10.
  • the water used to condense the water vapor is previously pre-heated by the heat released during condensation heat.
  • the preheated water then flows through the supply line 10 to the evaporator 12.
  • An additional heat input into the water flowing through the supply line 10 is then effected via the heat exchanger 5 in the system according to FIG.
  • the originating from the separator 3 hot waste water is thus fed to the heat exchanger 5, in which a part of its heat is discharged to the circulating between the evaporator 12 and the condenser 11 water. This is followed by a relaxation at the pressure reducer 8 and then the introduction in the water cycle of the thermal separator comprising the evaporator 12 and the condenser 11.
  • the evaporation process in the evaporator 12 and also the condensation process in the condenser 11 are carried out in the present case preferably at temperatures below the boiling point.
  • the heat exchangers will be used shear. 5
  • the relaxation on the heat exchanger 5 and also on the pressure reducer 8 ensures a reduction in the pressure of the output side of the separator 3 at a high pressure contaminated water.
  • the plant 1 shown in FIG. 2 corresponds in essential parts to that shown in FIG. However, here is the Einmün- point 9 of the pressure reducer 8 having line 7 downstream of the heat exchanger 5 in the supply line 10 is provided. Accordingly, the COM ⁇ Mende from the separator 3 contaminated water flows through the heat exchanger 5 only once and not as in the system 1 according to FIG 1 twice.
  • the contaminated water is supplied via the valve 6 and the line 7 to the pressure reducer 8 and then di ⁇ rect, ie without renewed heating at the heat exchanger 5 via the inlet 13 to the water distributor 14 of the evaporator 12 supplied.
  • Such a process scheme is favorable, for example, when the separator 3 leaving, contaminated water is relatively hot and therefore requires no further heating after relaxing the pressure reducer 8.
  • the entering at the mouth Steep 9 in the supply line 10 What ⁇ ser may very well be mixed with the coming from the condenser 11 water and this up heat coming from the condenser 11 water. Then there is another, direct heat transfer, without the need for another heat exchanger needs to be provided.
  • the plant 1 shown in FIG. 3 essentially corresponds to that shown in FIG.
  • a means for acquiring mechanical energy is provided instead of the pressure Minde ⁇ RERS 8, such as a turbine 30.
  • the obtained when flowing through the turbine 30, mechanical energy 22 may be used for example, for operating the blower 26 and / or the pump.
  • the potential energy of the polluted water leaving the separator 3 under high pressure of, for example, 50 bar can be utilized well via the device embodied by way of example as the turbine 30.
  • the system 1 can also be designed in several stages.
  • An example of such a system 1 is shown schematically in FIG.
  • the contaminated water coming from the separator 3 via the line 4 is first fed to the heat exchanger 5 and gives off heat there.
  • the contaminated wastewater in the present example three-stage system 1 flows through a second heat exchanger 32 and through a third heat exchanger 33, wherein each heat is emitted.
  • the contaminated water which is then already comparatively largely cooled then flows via the inlet 13 into the evaporator 12 and from there via the outlet 19 and the connecting line 21 into the condenser 11.
  • the evaporator 12 and the condenser 11 belong to a stage 43 of the system - Ge 1, by which one of the present three thermal
  • the radiator 23 may be provided.
  • the water heated by the condenser 11 flows - gegebe ⁇ appropriate, after intermediate cooling, to a further cooler 34 - into a condenser 35 which is associated with a further stage 36 or separating device Appendix 1.
  • a evaporator 37 is provided in this stage 36 and a evaporator 37 is provided.
  • the water flows to a condenser 38 of a first stage 39 or first thermal separator of the system 1.
  • the guidance of the air flow in the individual stages 39, 36, 43 of the system 1 is shown in FIG simplicity ⁇ is not Darge.
  • Zvi ⁇ rule may be provided for intermediate cooling, a further cooler 40 to the capacitor 35 of the second stage 36 and the capacitor 38 of the first stage.
  • the water leaving the condenser 38 flows through the heat exchanger 5, that is to say through that heat exchanger which has the highest temperature of the three heat exchangers 5, 32, 33 shown in FIG. 4 for heating purposes.
  • the water heated in this heat exchanger 5 is fed to a vaporizer 41 of the first stage 39 of the system 1.
  • the water leaving this evaporator 41 flows through the second heat exchanger 32 to the evaporator 37 of the second stage 36.
  • each evaporator 41, 37, 12 can be comparatively low temperature differences within the individual stages 39, set 36, 43.
  • a great deal can be the input side of each evaporator 41, 37, 12 related to the Availability checked ⁇ supply heat for heating the air flow and thus used for providing steam.
  • the separation means in the form of stages 39, 36, 43 with the respective evaporators 41, 37, 12 and capacitors 38, 35, 11 thus serve to recover product water with a particularly high efficiency of the system 1.
  • the waste heat of the effluent from the separator 3 water or mixture is used as a heat source for the convectionally driven evaporation ⁇ ge process.
  • the plant 1 allows the use of the heat of the separated water and also an internal heat recovery via the at least one capacitor 11, 35, 38.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (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)

Abstract

L'invention concerne une installation (1) pour le traitement d'une eau polluée obtenue lors de l'extraction d'un combustible fossile, et contenant une énergie géothermique. Pour séparer les polluants de l'eau produite à obtenir à partir de l'eau est prévu au moins un dispositif de séparation qui comprend au moins un évaporateur (12) et au moins un condensateur (11). Par l'intermédiaire de l'évaporateur (12) ou des évaporateurs et du condensateur (11) ou des condensateurs, l'eau présentant les polluants peut être conduite dans un circuit. Le ou les dispositifs de séparation sont affectés à au moins un échangeur de chaleur (5), dans lequel l'eau contenant l'énergie géothermique peut être introduite comme milieu de chauffage. Au moyen de l'échangeur de chaleur (5) ou des échangeurs de chaleur, au moins une partie de l'énergie géothermique peut être amenée à l'évaporateur (12) ou aux évaporateurs, et l'eau présentant les polluants peut être transférée. En outre, l'invention concerne un procédé de traitement de l'eau.
PCT/EP2014/060040 2013-06-05 2014-05-16 Installation et procédé de traitement d'eau Ceased WO2014195110A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102013210425.1A DE102013210425A1 (de) 2013-06-05 2013-06-05 Anlage und Verfahren zum Aufbereiten von Wasser
DE102013210425.1 2013-06-05

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WO2014195110A1 true WO2014195110A1 (fr) 2014-12-11

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PCT/EP2014/060040 Ceased WO2014195110A1 (fr) 2013-06-05 2014-05-16 Installation et procédé de traitement d'eau

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2017021884A1 (fr) * 2015-08-03 2017-02-09 Nereid Sa Système de distillation d'eau
CN106396229A (zh) * 2016-10-21 2017-02-15 成都朵猫文化传播有限公司 一种医院污水处理箱
CN111410252A (zh) * 2020-04-15 2020-07-14 平湖爱驰威汽车零部件有限公司 一种锻件清洗产生废水的油水分离系统

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Publication number Priority date Publication date Assignee Title
DE102014212973A1 (de) * 2014-07-03 2016-01-07 Siemens Aktiengesellschaft Verschaltungskonzept für eine thermische Aufbereitungsanlage
DE102016214019A1 (de) * 2016-07-29 2018-02-01 Siemens Aktiengesellschaft Vorrichtung zum Abtrennen von Produktwasser aus verunreinigtem Rohwasser und Verfahren zum Betrieb dieser Vorrichtung

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