WO2016000862A1 - Concept de câble d'une installation de préparation thermique - Google Patents

Concept de câble d'une installation de préparation thermique Download PDF

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Publication number
WO2016000862A1
WO2016000862A1 PCT/EP2015/060400 EP2015060400W WO2016000862A1 WO 2016000862 A1 WO2016000862 A1 WO 2016000862A1 EP 2015060400 W EP2015060400 W EP 2015060400W WO 2016000862 A1 WO2016000862 A1 WO 2016000862A1
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WO
WIPO (PCT)
Prior art keywords
modules
liquid
module
condensate
heat
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/EP2015/060400
Other languages
German (de)
English (en)
Inventor
Thomas Hammer
Markus Ziegmann
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 WO2016000862A1 publication Critical patent/WO2016000862A1/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
    • B01D1/14—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
    • B01D1/0011—Heating features
    • B01D1/0058—Use of waste energy from other processes or sources, e.g. combustion gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/0088—Cascade evaporators
    • 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

Definitions

  • the present invention relates to a device and a method for recovering by means of thermal treatment of a portion of a mass flow of liquid emitted by a process with foreign substances contained, in particular wastewater, using waste heat of the process, in particular with temperatures below 100 ° C. ,
  • the decisive factor in the use of this physical process in addition to the thermodynamic equilibrium that is, the amount of water that can pass into the gas phase at a given temperature, especially the kinetics of the interlinked heat and mass transfer.
  • the relationship between the air temperature and the maximum absolute water content of the air is not linear and thus also the mass transport limitation is not constant.
  • the air and water pass through the passage of the evaporator, different ratios of air and water flow are advantageous.
  • the primary solvable problem is thus a meaningful subdivision of the plant, in particular of the evaporator, in several stages and an efficient interconnection of the material flows between and within the stages.
  • a common method which operates the thermal water treatment by means of evaporation at atmospheric pressure in a downdraft evaporator with air in countercurrent combined with waste water cooled condensers for condensation of the clean product water while recovering the heat of evaporation is known.
  • DE102008051731A1 discloses an apparatus for separating foreign substances contained in a liquid with a first closed loop leading the liquid in a first direction, in which at least one unit comprising a vaporizer and a condenser and a heat exchanger are located; a second, a heat transfer fluid in an opposite direction leading closed circuit in which the condenser and the heat exchanger are; Means for removing the contaminants accumulating in the evaporator; Means for introducing one of the mass of the discharged foreign matter and the discharged condensate corresponding
  • Mass of liquid containing foreign matter and means for discharging the condensate formed in the condenser of the or at least one of the units, the liquid containing the impurities contained therein being introduced through the one side of the heat exchanger in the warmer heated therein and partially circulating in the evaporator liberated enriching foreign substances, in this cooled liquid is fed back to one side of the heat exchanger; wherein the heat transfer fluid passed through the other side of the heat exchanger, cooled in this supplied to one side of the capacitor and the warmed in the condenser heat transfer fluid to the other side of the heat exchanger is fed back, and wherein in or in the unit (s) a carrier gas through the evaporator with the absorption of heat and moisture and by the condenser with release of heat and moisture - and thus release of the condensate - circulates.
  • the object is achieved by a device according to the main claim and a method according to the independent claim.
  • an apparatus for separating foreign substances contained in a liquid wherein the liquid is guided in a direction in a circle in which a evaporator and a condenser unit and an upper and a lower heat exchanger and a pump in which a carrier gas is circulated in the unit through the evaporator with the absorption of heat and moisture and through the condenser with release of heat and moisture, and thus release of the condensate, whereby the liquid with the foreign substances contained in it is passed through the upper heat exchanger, warmed up in this and introduced into the evaporator and cooled in the evaporator by the evaporation process and at the same time enriched with impurities, liquid is supplied to the lower heat exchanger and further cooled in this, wherein then the liquid of one side of the capacitor z supplied and the liquid warmed up in the condenser is fed back to the upper heat exchanger, the circuit together with means for discharging the condensate formed in the condenser of the unit and the
  • the enriched solution is constantly pumped in circulation by condenser and evaporator.
  • a method for separating foreign matter contained in a liquid wherein the liquid is guided in a direction in a circle in which a evaporator and a condenser unit and an upper and a lower heat exchanger and a pump are in which a carrier gas is circulated in the unit through the evaporator with the absorption of heat and moisture and through the condenser with release of heat and moisture - and thus release of the condensate - with the liquid with the foreign matter contained therein being passed through the upper heat exchanger ,
  • liquid is supplied to the lower heat exchanger and further cooled in this, wherein thereafter the liquid of one side of the capacitor and the liquid warmed in the condenser is returned to the upper heat exchanger, the circuit together with means for discharging the condensate formed in the condenser of the unit and for partially dis
  • the modules can be thermally coupled to the heat source in such a way that the respective upper heat exchangers can be successively positioned starting from a low to a high temperature level along an external heat flow in this module sequence and the respective liquids with those contained in them Foreign substances are heatable.
  • the modules can be thermally coupled to the heat sink such that the respective lower heat exchangers can be positioned successively from an low to a high temperature level along an external coolant flow in the module sequence and the respective liquids enriched with foreign substances can be cooled are.
  • the modules can be materially coupled to one another in such a way that the condensate produced from each module individually and the liquid enriched with foreign substances of all modules can be discharged from the last module and the sum of the liquids discharged by liquid from the sump of the respective previous module are replaceable, wherein in the first module, the discharged liquids by fresh liquid in which the foreign substances are originally included, replaceable.
  • the means for discharging the condensate produced in each module may have a pump.
  • the means for discharging the respective foreign substances accumulating in each module can have pumps downstream of a respective module.
  • the means for introducing one of the mass of the discharged condensate and the discharged foreign matter corresponding mass of the liquid in which foreign substances are contained have a module upstream of pumps.
  • the number of modules can be selected depending on a temperature and a mass flow of the heat source.
  • a relatively large number of modules can be selected.
  • a relatively small number of relatively larger sized modules can be selected.
  • the number of modules can be selected depending on a demand of the amount of condensate in relation to the temperature and the mass flow of the heat source and / or cooling water.
  • the rear modules in the module sequence can be designed such that they provide a relatively large gain output ratio.
  • GOR means "gain output ratio”. This correlates the amount of condensate Ko or product water with the part of the waste heat flow Ql.
  • the rear modules in the module sequence can have relatively large evaporator and capacitor surfaces and / or a relatively large circulated carrier flow.
  • FIG. 1 shows an embodiment of a conventional
  • FIG. 1 shows an embodiment of a conventional interconnection.
  • FIG. 1 shows a flow chart.
  • the temperatures given there are exemplary values in order to better understand the path of the water.
  • the system shown consists of three modules, each containing a condenser on the right side and a vaporizer on the left side.
  • the circulating in the system wastewater flows from the coldest point of the system, ie of 33 ° C, after the heat exchanger bottom right, as a coolant through the condenser of module 1, thereby absorbs heat (48 ° C), is used as a coolant in the Conductor of module 2, which is generally operated at higher temperatures, absorbs additional heat (63 ° C) and is then passed as a coolant through the condenser of the warmest module 3 (78 ° C).
  • the preheated wastewater is further heated in an external heat exchanger by the waste heat source, namely to the maximum temperature, in this example 87 ° C. From there, the water is sequentially with falling temperature on the
  • the wastewater is externally cooled, to be used again as a coolant in the condenser of module 1.
  • the air which acts as a carrier medium for the water vapor (water absorption and heating in the evaporator, water release and cooling in the condenser), does not pass sequentially through the modules as the wastewater, but circulates within the individual modules in countercurrent to the water flow.
  • the amount of condensate (product water) that is produced, as well as the amount of concentrated wastewater that needs to be removed to avoid precipitation, blockage of piping, etc., must be replaced with new wastewater.
  • the dimensioning of the individual stages can be designed separately, as well as the circulating within each stage airflow.
  • the waste water volume flow in all modules is the same, on the other hand, the heat source (and the cooling source) is used only at one point of the system, whereby the temperature difference within the heat source and thus the usable heat is limited.
  • FIG. 2 shows an embodiment of a device according to the invention.
  • This device according to the invention serves to separate foreign substances Fr contained in a liquid F.
  • the illustration according to FIG. 2 has three modules 1, 2 and 3. These three separate Modi, Mod2 and Mod3 Modules are the same or similar in their construction. These modules have a heat source Wq, a heat sink Ws, and a similar coupling or interconnection. For example, starting from the right module modes, its structure will be described as follows.
  • the liquid F is guided in one direction in a circle in which a unit comprising an evaporator V and a condenser K and an upper and a lower heat exchanger Wo and Wu and a pump PI are located.
  • a carrier gas circulates through the evaporator V while absorbing heat and moisture and through the condenser K with release of heat and moisture and thus release of the condensate Ko.
  • the liquid F is guided with the foreign substances Fr contained therein through the upper heat exchanger Wo, in this warmed up and introduced into the evaporator V and cooled in the evaporator V by the evaporation process and at the same time with
  • the embodiment of a device according to the invention according to FIG. 2 shows an interconnection of three separate modules Modi, Mod2 and Mod3, wherein these components have the same construction and are coupled and / or interconnected to a heat source Wq, to a heat sink Ws and to one another.
  • the Modi, Mod2 and Mod3 modules are similarly thermally coupled to the heat source Wq shown at the top left, such that the respective upper heat exchangers Wo extend from a low temperature level Tkl to a high temperature level Tgl of the heat source Wq along an external heat flow Ql in this Module sequence are positioned successively and thereby the respective liquids F can be warmed up with the foreign substances Fr contained in them.
  • reference numeral 1 denotes a main entrance for a liquid F, the contained Foreign matter Fr have to be separated.
  • Such a liquid F can be taken from an industrial process, which additionally provides the heat source Wq, which is at a certain temperature level Tgl.
  • Reference numeral 2 in Figure 2 identifies this available heat source Wq with the high temperature level Tgl.
  • FIG. 2 additionally shows that the modules Modi, Mod2 and Mod3 can be thermally coupled to a heat sink Ws such that the respective lower heat exchangers Wu start from a low to a high temperature level from Tk2 to Tg2 along an external coolant flow Q2 in the module Sequence can be successively positioned and the respective partially enriching foreign matter for freed liquids F can be cooled.
  • Reference numeral 3 shows the small temperature level Tk2 of the heat sink Ws and the flow Q2 of the external refrigerant, which heats up to the high temperature level Tg2 shown by the reference numeral 7.
  • FIG. 2 further shows that the Modi, Mod2 and Mod3 modules can be connected to one another in such a way that the respectively produced condensate Ko can be transported individually from each module to a condensate collection point 5 by means of a pump P2.
  • the respectively accumulating impurities Fr and the mass of the discharged enriched solution of all modules can be removed from the last module Mod3.
  • Solution can be replaced by liquid F from a sump of a respective previous module, wherein in the first module modes the produced condensate Ko and discharged from the sump to the following module enriched with foreign matter Fr liquid F by fresh wastewater or fresh enriched with impurities Fr liquid F is replaceable, are included in the foreign matter Fr.
  • the means M1 for discharging the condensate produced in each module has one Pump P2 on.
  • the means M2 for discharging the respective foreign substances Fr accumulating in each module have downstream pumps P3 to a respective module.
  • Reference numeral 6 denotes the main output for each accumulating
  • the temperatures shown in FIG. 2 merely represent examples. Furthermore, the number of interconnected separate modules can be greater than or equal to 2 and basically arbitrary.
  • FIG. 2 shows an embodiment of an inventive interconnection of three modules here. Not only is an air stream circulated as an example of a carrier gas within the modules, but also a waste water stream, which has been generally referred to herein as liquid F.
  • Each Modi, Mod2 and Mod3 module is therefore to be regarded as a separate plant.
  • the externally available waste heat from the heat source Wq can now be tapped at each module at different temperature levels by means of the upper heat exchanger, since an output current of a capacitor K, unlike the interconnection of Figure 1 is no longer conducted as a coolant in a capacitor K of a circuit-technically following module but in the evaporator V of the same module.
  • the available waste heat of the heat source Wq can thus be used more efficiently.
  • significantly higher temperature gradients can be achieved within the individual Modi, Mod2, ... modules from head to tail, thereby increasing the amount of condensate Ko produced.
  • An inventive coupling of modules can be accomplished in two ways.
  • a thermal coupling is performed.
  • a material coupling is carried out by replacing the condensate Ko produced per module and the removed, foreign-matter-enriched liquid with fresh wastewater or the foreign-matter-enriched liquid from the bottom of the preceding one.
  • the missing water or the missing liquid F can be replaced by fresh waste water or fresh liquid F to be cleaned.
  • the concentrated wastewater is removed from the overall process to an outlet 6.
  • the entire system can be expanded as desired with mod modules.
  • the individual mod modules can be designed differently, depending on what the boundary condition is.
  • the waste heat of the heat source Wq for example, at high temperatures, for example at 95 ° C, and a relatively low mass flow before, so the number of modules can be increased, as a result, the heat source Wq can be utilized to a greater extent.
  • at high waste heat mass flows with comparatively low temperatures, for example at 70 ° C makes a larger-sized and thus thermodynamically more efficient system with fewer stages or with the solution shown in Figure 2 makes sense.
  • the need for treated water or condensate Ko in relation to the heat source WQ and the availability of cooling water of the heat sink Ws play a role in the decision for a specific interconnection or for the choice of the number of modules Mod.
  • the advantage of a device according to the invention or of a method according to the invention lies with the same boundary conditions with respect to the heat source WQ, depending on the temperature. Turn level Tgl in a significantly higher product water flow or condensate Ko.
  • GOR gain output ratio
  • Heat source Wq is therefore certainly causes a higher efficiency.
  • FIG. 3 shows an exemplary embodiment of a method according to the invention.
  • the first step S1 illustrates that a plurality of separate component-like modules can be coupled to one another in the same way.
  • the modules are thermally coupled to the heat source in such a way that the respective upper heat exchangers are successively positioned from a low to a high temperature level along an external heat flow in this module sequence and the respective liquids with the in warmed up with foreign substances contained in them.
  • the modules are thermally coupled to the heat sink such that the respective lower heat exchangers are successively positioned from a low to a high temperature level along an external coolant flow in the module order and the respective and partly accumulating impurities cooled liquids are cooled.
  • the modules are materially coupled to one another in such a way that the condensate produced is removed from each module individually and the respective enriching foreign substances of all modules are removed from the last module and replaced by liquid from a sump of a respective preceding module, wherein in the first module the produced condensate is replaced by fresh liquid in which foreign matter is contained.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

La présente invention concerne un dispositif et un procédé de séparation de matières étrangères (Fr) contenues dans un liquide (F), des modules séparés (Mod1, Mod2, Mod3) étant formés à chaque fois et une pluralité de modules identiques en termes de composants étant accouplés de la même façon à une source de chaleur (WQ), à un dissipateur de chaleur (WS) et les uns aux autres.
PCT/EP2015/060400 2014-07-03 2015-05-12 Concept de câble d'une installation de préparation thermique Ceased WO2016000862A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102014212973.7 2014-07-03
DE102014212973.7A DE102014212973A1 (de) 2014-07-03 2014-07-03 Verschaltungskonzept für eine thermische Aufbereitungsanlage

Publications (1)

Publication Number Publication Date
WO2016000862A1 true WO2016000862A1 (fr) 2016-01-07

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Application Number Title Priority Date Filing Date
PCT/EP2015/060400 Ceased WO2016000862A1 (fr) 2014-07-03 2015-05-12 Concept de câble d'une installation de préparation thermique

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DE (1) DE102014212973A1 (fr)
WO (1) WO2016000862A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102016214019A1 (de) * 2016-07-29 2018-02-01 Siemens Aktiengesellschaft Vorrichtung zum Abtrennen von Produktwasser aus verunreinigtem Rohwasser und Verfahren zum Betrieb dieser Vorrichtung

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3345272A (en) * 1965-05-14 1967-10-03 Richard A Collins Multiple effect purification of contaminated fluids by direct gaseous flow contact
FR2536738A1 (fr) * 1982-11-26 1984-06-01 Mitsubishi Electric Corp Appareil de dessalement
WO1988006054A1 (fr) * 1987-02-11 1988-08-25 Sten Zeilon Procede servant a separer un composant volatil d'un melange en utilisant un gaz porteur pour le transport de vapeur depuis un evaporateur jusqu'a un condenseur
WO2007128062A1 (fr) * 2006-05-05 2007-11-15 Newcastle Innovation Limited Appareil et procede de dessalement
DE102008051731A1 (de) 2008-10-15 2010-04-22 Terrawater Gmbh Vorrichtung zum Abtrennen von einer Flüssigkeit gelösten Fremdstoffen
US20100275600A1 (en) * 2007-11-08 2010-11-04 Speirs Brian C System and method of recovering heat and water and generating power from bitumen mining operations
US20120241308A1 (en) * 2009-09-21 2012-09-27 Phoenix Water Thermal Distillation System and Process
US20120292176A1 (en) * 2010-02-10 2012-11-22 Basf Se Water treatment process

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3860492A (en) * 1973-06-27 1975-01-14 Jr Alvin Lowi Liquid separation system
AU6088699A (en) * 1998-10-01 2000-04-26 Klaus Wolter Device and method for obtaining water for industrial use from untreated water
DE102004005689A1 (de) * 2004-02-05 2005-08-25 Vinz, Peter, Dr. Ausdampfverfahren zur Reinigung und/oder Aufkonzentrierung verunreinigter Flüssigkeiten
DE102013210425A1 (de) * 2013-06-05 2014-12-11 Siemens Aktiengesellschaft Anlage und Verfahren zum Aufbereiten von Wasser

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3345272A (en) * 1965-05-14 1967-10-03 Richard A Collins Multiple effect purification of contaminated fluids by direct gaseous flow contact
FR2536738A1 (fr) * 1982-11-26 1984-06-01 Mitsubishi Electric Corp Appareil de dessalement
WO1988006054A1 (fr) * 1987-02-11 1988-08-25 Sten Zeilon Procede servant a separer un composant volatil d'un melange en utilisant un gaz porteur pour le transport de vapeur depuis un evaporateur jusqu'a un condenseur
WO2007128062A1 (fr) * 2006-05-05 2007-11-15 Newcastle Innovation Limited Appareil et procede de dessalement
US20100275600A1 (en) * 2007-11-08 2010-11-04 Speirs Brian C System and method of recovering heat and water and generating power from bitumen mining operations
DE102008051731A1 (de) 2008-10-15 2010-04-22 Terrawater Gmbh Vorrichtung zum Abtrennen von einer Flüssigkeit gelösten Fremdstoffen
US20120241308A1 (en) * 2009-09-21 2012-09-27 Phoenix Water Thermal Distillation System and Process
US20120292176A1 (en) * 2010-02-10 2012-11-22 Basf Se Water treatment process

Also Published As

Publication number Publication date
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