EP3472104A1 - Dispositif de séparation d'eau produite présente dans de l'eau brute contaminée et procédé permettant de faire fonctionner ledit dispositif - Google Patents

Dispositif de séparation d'eau produite présente dans de l'eau brute contaminée et procédé permettant de faire fonctionner ledit dispositif

Info

Publication number
EP3472104A1
EP3472104A1 EP17740344.1A EP17740344A EP3472104A1 EP 3472104 A1 EP3472104 A1 EP 3472104A1 EP 17740344 A EP17740344 A EP 17740344A EP 3472104 A1 EP3472104 A1 EP 3472104A1
Authority
EP
European Patent Office
Prior art keywords
product water
condenser
water
evaporator
raw water
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Withdrawn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
EP17740344.1A
Other languages
German (de)
English (en)
Inventor
Andreas Büttner
Thomas Hammer
Markus Ungerer
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
Original Assignee
Siemens AG
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 filed Critical Siemens AG
Publication of EP3472104A1 publication Critical patent/EP3472104A1/fr
Withdrawn legal-status Critical Current

Links

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
    • C02F1/048—Purification of waste water by evaporation
    • 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
    • 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
    • B01D5/0027—Condensation of vapours; Recovering volatile solvents by condensation by direct contact between vapours or gases and the cooling medium
    • B01D5/003—Condensation of vapours; Recovering volatile solvents by condensation by direct contact between vapours or gases and the cooling medium within column(s)
    • 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
    • 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
    • B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
    • B01D5/009—Collecting, removing and/or treatment of the condensate
    • 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

Definitions

  • the invention relates to a device for separating product water, which is obtained by condensation, from raw water, which consists of a mixture of water and impurities.
  • This device has a gas circulation, which is provided for a process gas and in a
  • Evaporator for the raw water and a condenser for the product water are connected in series, ie, in each case be alterna ⁇ selnd run through.
  • the evaporator has a feed for the raw water and a discharge for a concentrate, wherein the concentrate has a higher concentration of impurities to be separated compared to the raw water.
  • the impurities to be separated have no lower boiling point than water and therefore remain in the raw water.
  • the product water is drained through an outlet of the condenser.
  • the invention relates to a method for separating product water, which is obtained by condensation, from raw water, which consists of a mixture of water and impurities.
  • a gas cycle is operated with a process gas, wherein in the gas circuit ⁇ a vaporizer for the raw water and a capacitor for the product water are connected in series.
  • the evaporator is supplied via a feed with the raw water and a discharge in the evaporator, a concentrate is removed, which in comparison to the raw water on has a higher concentration of impurities to be separated.
  • the condenser can then be removed via an outlet purified product water.
  • a device and a cleaning method suitable for this device are known and can be found for example in DE 10 2014 217 281 AI.
  • the operation of the device and the method according to this document will also be described in more detail with reference to FIG.
  • This method works on the principle of convective assisted evaporation of water in a downdraft evaporator in countercurrently flowing air.
  • the temperature of the downflowing in Verdun ⁇ ter water decreases from top to bottom, as the water is removed by evaporation and heat transfer to the air flowing against water.
  • the clean product in the form of water vapor is then condensed out in a condenser, which is preferably cooled by the raw water, the evaporation heat being released being supplied to the raw water.
  • the humidified gas stream can for example be fed to a tube bundle heat exchanger in order to cool down there and to condense the product water.
  • This embodiment allows a direct use of the raw water as a cooling medium to ei ⁇ ne internal heat recovery to ensure.
  • designed heat exchangers have inherently a heat transport through the tube walls, which is limited by the Ausbil ⁇ a dung-depleted water vapor gas layer near the surface of the heat exchanger.
  • ent ⁇ stands on the surface of the tubes, a water layer, which creates an additional heat transfer resistance.
  • corrosion-resistant materials that make the device more expensive must also be selected. This is due to both the high temperatures and the high oxygen content of the media.
  • the object of the invention is to develop a device and a method of the type mentioned at the outset such that on the one hand this enables efficient Kondensa ⁇ tion of the product water and on the other hand unemp ⁇ insensitive to the corrosive properties of the condensate.
  • the capacitor is designed in a construction principle of direct condensation. This means that the product water from the gas stream is condensed directly by cooling water is brought into direct contact with the gas flow in the gas circulation in the condenser.
  • a product water circuit ⁇ run is provided according to the invention, in which the condenser and a first heat exchanger for cooling the product water are connected in series.
  • an inlet is provided in a head of the condenser and an outlet in a foot of the condenser.
  • a flow direction from the foot of the condenser to the head of the condenser ie directed counter to the gas flow
  • a product water circuit in which the condenser and a first heat exchanger for cooling the product water are connected in series, so be alternated.
  • a direct condensation is carried out by introducing into the head of the condenser via an inlet the cool product water and in one foot of the condenser ⁇ tors the product water is discharged through an outlet again.
  • the process gas flows in the direction from the base of the condenser ⁇ tor to the head of the condenser, so that this is cooled in countercurrent to the supplied liquid product water while condensing product water from the process gas.
  • the cooling water and the damp come
  • Air flow or condensate in direct contact (principle of direct condensation).
  • a heat transfer via a separating medium is therefore not required, whereby the efficiency of the cooling advantageously increases.
  • the surface is provided for condensation by the product water itself, whereby a corrosive attack can be excluded.
  • the largest possible surface must for efficient mass and heat transfer as well as in Verdunster also be be ⁇ riding provided. This can be done in a conventional manner.
  • the cooling water can for example be injected into the condenser and / or be atomized.
  • the droplet size can be adjusted so that the droplets are small enough to provide sufficient surface area for heat transfer, but are large enough not to cause unnecessary energy expenditure in the atomizer.
  • Another possibility is the USAGE ⁇ dung of a package like this can also be used in Verdunster.
  • the package is used to increase the surface area and is acted upon by a film of the product water, wel ⁇ cher the surface of the package at the same time from corrosion protects, while a direct heat transfer takes place in the product ⁇ water.
  • the cooling water which is introduced into the condenser, inherently comes into direct contact with the product water, which is condensed from the gas circulation. Therefore, this must have at least the same quality. This is the reason for the measure according to the invention of cooling the product water and making it available to the condenser as cooling water in one cycle.
  • the condensed amount of product water can be removed from the circulation.
  • the evaporator is executed in a conventional manner in a construction principle in which the raw water and the gas of the gas circuit ⁇ run flow in the opposite direction, whereby this partially evaporated and in the remaining raw water a
  • the feed for the raw water and in one foot of the evaporator the discharge for the concentrate vorgese ⁇ hen, which are removed from the process in this way or can be recycled in a circuit to the evaporator on the head as raw water.
  • the conception of such a cycle is not absolutely necessary.
  • a flow direction from the base of the evaporator to the head of the evaporator is provided in the evaporator.
  • the gas circuit must also be guided such that the head of the condenser is connected to the base of the evaporator and the head of the evaporator to the base of the condenser.
  • Another advantage of using a capacitor according to the construction principle of direct condensation is that identical or at least similar construction components for the manufacture ⁇ ment of the condenser and the evaporator can be used. This simplifies and reduces manufacturing costs and therefore has economic advantages. Although a further heat exchanger must be provided because of the appli ⁇ dung of the direct condensation in the product water circuit, but this additional effort falls advantageously lower than the simplification of the structure of the capacitor, wherein in particular the A ⁇ rate materials can be reduced more expensive.
  • the first heat exchanger for cooling the product water is connected to a line for the raw water, wherein the line is guided after passing through the first heat exchanger for supplying the evaporator.
  • this line may be part of a circuit, wherein the raw water is at least partially removed from the Ver ⁇ dunster in the line as a concentrate.
  • the use of the raw water for cooling the product water allows the Auf ⁇ assumption of at least a portion of the heat necessary so that the ⁇ ses can be converted in the evaporator in a gaseous state.
  • the necessary heat of evaporation must be brought on ⁇ .
  • the first heat exchanger only serves to preheat the raw water, which absorbs, for example, process heat in the second heat exchanger ⁇ , which arises as waste in any process.
  • This waste heat can arise in ⁇ example, in industrial processes or in the Energyerzeu ⁇ supply, and therefore leads to a favorable energy balance in carrying out the method according to the invention or the use of the device according to the invention.
  • a third heat exchanger is provided in the product water circuit between the first heat exchanger and the inlet.
  • This advantageously serves for further cooling of the product water, which ensures that the temperature difference between the raw water coming from the evaporator and the product water fed into the condenser can be increased. This speeds up the process of recovering product water in the gas cycle. It is advantageous if the third heat exchanger is charged with a medium having ambient temperature, since then no additional energy expenditure is required for cooling this medium.
  • a particular embodiment of the invention is obtained when the evaporator and / or the condenser are constructed in multiple stages.
  • These stages may for example consist of packages, the surface of which serves for a downflow of the liquid medium (raw water or product water).
  • the liquid medium raw water or product water.
  • the package After the package fürlau- fen is collected the water and distributed uniformly over a ge ⁇ suitable means before it flows into the underlying package.
  • This device for distribution can also be used to atomize the liquid, in which case no packages are necessary.
  • the multi-stage advantageously allows Zvi ⁇ rule heating of the product water or intermediate cooling of the gas.
  • the device is constructed of several stages, wherein a plurality of Verdunster and Kondensa ⁇ gates are equipped in pairs, each with a product water circuit and a gas circuit.
  • a plurality of Verdunster and Kondensa ⁇ gates are equipped in pairs, each with a product water circuit and a gas circuit.
  • he ⁇ enter Verdunster each and a capacitor at least two pairs of arrays that can operate independently of each other in cooperating product water circuits and gas circuits.
  • Each of the stages operates at different operating temperatures, but when using more than two stages the adjacent stages work at staggered operating temperatures.
  • the neighborhood is thus defined in terms of the respective temperature differences in the product water cycle or in the gas cycle and not by any local neighborhood.
  • the invention provides that the Fischwas ⁇ ser Vietnamese adjacent stages are connected to a first connecting line, wherein more than two product water circuits and a plurality of first connecting lines are provided.
  • a second connecting line between the foot of one of the evaporator of a stage with a lower temperature level and the head of the evaporator egg ⁇ ner adjacent stage is provided with a higher temperature level.
  • a plurality of second connection lines can be used.
  • the first connection lines and the second connection lines advantageously allow the individual stages to communicate with each other by allowing product water as well as condensate or raw water to be passed from one stage with a cooler temperature level to an adjacent higher temperature level stage. This has the advantage that the thermal energy of the concerned
  • Fluids can be used in the stage with the higher temperature level, so that cooling is not required or at least not to the extent that would be required in the stage with the lower temperature level. This can advantageously further increase the efficiency of the process.
  • the second connecting lines each lead to the heads of the evaporator. If a cycle is provided for the raw water, a part of these connecting lines can also be formed by the line system of the circuit. To this end, has circulated a suitable feed point are vorgese ⁇ hen which guarantees a connection.
  • the heat transfer medium can achieve a cooling effect in each of the third heat exchangers.
  • a second heat exchanger is arranged, wherein the second heat exchanger adjacent stages by a fourth connecting line are connected.
  • connection line can advantageously be passed a heat transfer medium, which, for example, the process heat of an industrial process to the raw ⁇ gives water.
  • the fourth connecting line is advantageous first through the second heat exchanger for the hottest
  • the method specified above can be carried out particularly advantageous also on a device of the type described.
  • the associated advantages have already been mentioned in the Erläu ⁇ esterification of the device.
  • FIG. 1 shows a device for separating product water from raw water according to the prior art, on which a process for separating product water from raw water runs, as a schematic block diagram
  • Figure 2 shows an embodiment of the device according to the invention, on which an embodiment of he ⁇ inventive method is running, as a block diagram ⁇ image and
  • FIG. 3 shows an exemplary embodiment of the device according to the invention with two stages, on which an exemplary embodiment of the multi-stage method according to the invention runs, as a block diagram.
  • FIG. 1 a device with a gas circuit 11 and a raw water circuit 12 is shown. In both runs, a circle ⁇ Verdunster 13 and a capacitor 14 are connected in series, that is, these are traversed alternately.
  • the raw water and the process gas circulate in opposite directions, so that evaporation of the raw water into the evaporator 13 by the process gas from the gas circuit 11 occurs in opposite directions.
  • the raw water is conveyed by a pump 15 in the raw water circuit 12 and the gas (preferably air) through a blower 16 in the process gas cycle.
  • the respective flow directions are indicated by arrows.
  • the raw water is used in the condenser as the cooling medium, in which case product water from the Process gas is condensed out and thereby the raw water he warmed ⁇ .
  • the heated raw water is then further heated in a second heat exchanger 17, which is supplied via a connecting line 18 with a process heat of an industrial process leading heat transfer medium.
  • the thus heated raw water is then fed through a head 19 of the evaporator 13, wherein in the head 19, a trickling means 20 is provided which generates a mist 21 of small droplets.
  • the temperature of the raw water flowing down in this way decreases from the head 19 to a base 20 of the evaporator, because heat is extracted from the raw water by evaporation of product water and heat transfer to the process gas.
  • the temperature of the countercurrent process gas therefore rises from the foot 22 to the head 19, remains in stable operation with stationary conditions but always below the temperature of the raw water at je ⁇ Weils same height of the evaporator 13. This allows the process gas absorb more water vapor of the product water.
  • the raw water and the process gas thus form a countercurrent heat exchanger, which operates on the principle of direct evaporation.
  • the raw water thus passes through a feed 23 into the evaporator and is concentrated by evaporation of product water with respect to the impurities. It collects in the foot 22 of the evaporator 13 and leaves it through an outlet 24 as a concentrate.
  • This can either be of the device be removed via a removal line 25 as a concentrate K or a storage tank 26 is supplied to draw a further pass in the raw water circuit 12 to complete ⁇ .
  • Extracted concentrate K or evaporated product ⁇ water can be replaced via a feed line 27 by supplying new raw water R.
  • the raw water is further used to cool the condenser 14. In order to realize a sufficiently large temperature difference for this purpose, the raw water can be cooled by a fourth heat exchanger 28 before it the capacitor 14 is supplied.
  • the Pro ⁇ duktwasser from the process gas which is fed into a header 29, a ⁇ condensed.
  • the dryer process gas leaves the condenser 14 through a foot 30, while product water P is taken out via an outlet 31 in the condenser 14 and can be removed via a removal line 32.
  • the device according to FIG. 2 is largely constructed in the same way as the device according to FIG. 1, which results from the use of the same reference numerals. However, an essential difference is that a further circuit, namely a product water circuit 33 operated by a pump 99, is provided.
  • the condenser 14 is incorporated, wherein the product water is removed through the outlet 31 from the condenser 14 and is supplied after cooling through an inlet 34 in the head 29 of the condenser 14 again.
  • a Verrieselungsaku 20 is provided as in the Ver ⁇ dunster 13, wherein the process gas is opposite to the verrieselten product water flows from the foot 30 of the capacitor to the head 29 of the capacitor fourteenth
  • the process gas is opposite to the verrieselten product water flows from the foot 30 of the capacitor to the head 29 of the capacitor fourteenth
  • the con densed ⁇ product water collects in the foot 30th
  • the product water from the product water circuit 33 heats up during the condensation, it must be cooled after removal from the outlet 31.
  • first a first heat exchanger 35 is available, which is fed by the raw water in the raw water circuit 12. In this way, the raw water can absorb the heat that was withdrawn due to the evaporation in the evaporator 13.
  • the product water can pass through a third heat exchanger 36 in which it is further cooled by an external cooling source before it is fed back to the condenser 14 via the inlet 34. It would also be conceivable, depending on the differences in temperature, to cool the raw water externally and cool it with the cooling water. th raw water (not Darge ⁇ represents) the condensate circuit to cool.
  • the Verdunster 13 and the capacitor 14 is constructed in each case a plurality of stages, wherein each ⁇ wells two successively connected packs 37 find use in the Verdunster 13 and in the condenser fourteenth These can, as a heat transfer through the material due to the direct evaporation or direct condensation is not necessary, for example, a chemically very stable
  • each represents a hydrogen manifold 38 is provided which duktwasser the product or the raw water captures each and subsequently ⁇ hd distributed through a plurality of openings over the entire cross section of the evaporator 13 and condenser fourteenth
  • a structure of both the evaporator 13 and the capacitor 14 according to the dargestell ⁇ th in Figure 1 structure is possible, wherein the liquid is trickled or atomized according to FIG.
  • Figure 3 shows a structure of the device in two stages 39a, 39b. Of course, more than the two stages shown can be used, with the statements made below can also be applied to three and multi-stage devices.
  • the pumps 15, blowers 16 and storage tanks 26 shown in FIGS. 1 and 2 have been omitted, but are also present to ensure the function of the device according to FIG.
  • the valves used in the figures 1 to 3 are not explained in detail and therefore not provided with reference numerals. The opening and closing of these valves depends on the respective functional state described and therefore results automatically.
  • the step 39a and the step 39b function for GE ⁇ taken as well as the device according to FIG 2, even if in the evaporators 13a, 13b and capacitors 14a, 14b, only one package 37 is provided in each case.
  • the stages 39a, 39b each have a raw water circuit 12a, 12b, a gas circuit IIa, IIb and a product water circuit 33a, 33b.
  • the Rohwas ⁇ water circuit 12a and the raw water circuit 12b respectively towards ⁇ ter the Verdunster 13a, 13b tung 40 via a second Mattslei- interconnected.
  • the raw water R is fed via the feed line 27 in the raw water circuit 12a and leaves this concentrated on the second connecting line 40 to the raw water circuit 12b supplied ⁇ leads.
  • a further concentration of impurities takes place in the evaporator 13b, wherein this concentrate K can be removed from the device via the extraction line 25.
  • the two product water circuits 33a, 33b are connected to one another via a first connecting line 41.
  • a removal of product water takes place behind the first heat exchanger 35 in the product water circuit 33a and is the Pro ⁇ duktwassernikank 33b behind the third heat exchanger 36 (or the first heat exchanger 35, not shown) of the product water circuit 35b supplied again. In this way, the product water recovered in the condenser 14a leaves the product water circuit 33a.
  • the forwarding of product water and raw water via the second connecting line 40 or the first Germanslei ⁇ device 41 advantageously allows this raw water or Pro ⁇ duktwasser from the stage 39a with a total cooler operating temperature in the stage 39b with a higher overall operating temperature where the thermal energy stored in the product water or raw water can be used. This reduces the overall effort associated with the cooling of raw water or product water is connected in the manner already described.
  • the second heat exchangers 17, which are housed in the raw water circuits 12a, 12b, are connected in series via the four ⁇ te connecting line 18, such that first the second heat exchanger 17 in the hotter stage 39b and then the second heat exchanger 17th in the cooler stage 39a (etc. at more than two stages).
  • the third heat exchangers 36 in the product water circuits 33a, 33b can be connected in series by a third connecting line 43, such that first the third heat exchanger 36 in the cooler product water circuit 33a and then the third heat exchanger 36 in the warmer product water circuit 33b (etc in more than two stages).
  • the heat exchange media are advantageously used optimally by the respective residual heat or residual cold in the adjacent stages 36a, 36b is still delivered.

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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)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

L'invention concerne un dispositif de séparation d'eau produite (P) qui a été récupérée par condensation dans un condenseur (14). Cette eau est récupérée à partir d'eau brute (R) qui est composée d'un mélange d'eau et d'impuretés et qui est concentrée ou extraite dans un évaporateur (13). Selon l'invention, à la fois l'évaporateur (13) et le condenseur (14) assurent une condensation directe ou une évaporation directe, un gaz de traitement étant guidé dans un circuit de gaz de traitement (11) d'un pied (22, 30) vers une tête (29, 19) de l'évaporateur (13) et du condenseur (14). Le fait que les fluides entre lesquels un échange de chaleur doit avoir lieu soient en contact direct permet avantageusement un fonctionnement très efficace du dispositif, l'utilisation d'éléments identiques permettant également de réduire les coûts en composants. Il est en outre possible de réduire de manière avantageuse le nombre de composants du dispositif qui sont exposés au milieu corrosif de l'eau brute. L'eau concentrée ou extraite est retirée du dispositif sous la forme d'un concentré (K). Outre le dispositif, l'invention concerne également un procédé permettant de le faire fonctionner.
EP17740344.1A 2016-07-29 2017-07-06 Dispositif de séparation d'eau produite présente dans de l'eau brute contaminée et procédé permettant de faire fonctionner ledit dispositif Withdrawn EP3472104A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102016214019.1A DE102016214019A1 (de) 2016-07-29 2016-07-29 Vorrichtung zum Abtrennen von Produktwasser aus verunreinigtem Rohwasser und Verfahren zum Betrieb dieser Vorrichtung
PCT/EP2017/066851 WO2018019534A1 (fr) 2016-07-29 2017-07-06 Dispositif de séparation d'eau produite présente dans de l'eau brute contaminée et procédé permettant de faire fonctionner ledit dispositif

Publications (1)

Publication Number Publication Date
EP3472104A1 true EP3472104A1 (fr) 2019-04-24

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EP17740344.1A Withdrawn EP3472104A1 (fr) 2016-07-29 2017-07-06 Dispositif de séparation d'eau produite présente dans de l'eau brute contaminée et procédé permettant de faire fonctionner ledit dispositif

Country Status (5)

Country Link
US (1) US20190161365A1 (fr)
EP (1) EP3472104A1 (fr)
CN (1) CN109641762A (fr)
DE (1) DE102016214019A1 (fr)
WO (1) WO2018019534A1 (fr)

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CN110292786A (zh) * 2019-07-29 2019-10-01 潍坊益华化工有限公司 一种巯基乙酸异辛酯连续精馏装置与工艺
IT201900015291A1 (it) 2019-08-30 2021-03-02 Distillerie Mazzari S P A Impianto e processo per la concentrazione dell’acido tartarico
IT201900015288A1 (it) 2019-08-30 2021-03-02 Distillerie Mazzari S P A Impianto e processo per la concentrazione dell’acido tartarico

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DE102011081015A1 (de) * 2011-08-16 2013-02-21 Siemens Aktiengesellschaft Verfahren zur Wiederaufbereitung eines Abwassers und Wasseraufbereitungsvorrichtung
DE102013210425A1 (de) * 2013-06-05 2014-12-11 Siemens Aktiengesellschaft Anlage und Verfahren zum Aufbereiten von Wasser
WO2015048878A1 (fr) * 2013-10-02 2015-04-09 Innocorps Research Corporation Système et procédé de décontamination de solvant
DE102013227061A1 (de) * 2013-12-23 2015-06-25 Siemens Aktiengesellschaft Verfahren zur Abtrennung von Wasser aus einem Wasser enthaltenden Fluidgemisch
DE102014212973A1 (de) * 2014-07-03 2016-01-07 Siemens Aktiengesellschaft Verschaltungskonzept für eine thermische Aufbereitungsanlage
DE102014217281A1 (de) 2014-08-29 2016-03-03 Siemens Aktiengesellschaft Verfahren zur Abtrennung von Wasser aus einem Wasser und wenigstens eine flüchtige saure und/oder basische Substanz enthaltenden Gemisch
DE102014217280A1 (de) * 2014-08-29 2016-03-03 Siemens Aktiengesellschaft Verfahren und Anordnung einer Dampfturbinenanlage in Kombination mit einer thermischen Wasseraufbereitung
CN105344119A (zh) * 2015-11-30 2016-02-24 浙江奇彩环境科技有限公司 一种低温喷淋蒸发的废水处理装置及废水处理方法

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DE102016214019A1 (de) 2018-02-01
US20190161365A1 (en) 2019-05-30
CN109641762A (zh) 2019-04-16

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