WO2000053533A1 - Method for treating an aqueous waste stream containing salts - Google Patents
Method for treating an aqueous waste stream containing salts Download PDFInfo
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- WO2000053533A1 WO2000053533A1 PCT/EP2000/001544 EP0001544W WO0053533A1 WO 2000053533 A1 WO2000053533 A1 WO 2000053533A1 EP 0001544 W EP0001544 W EP 0001544W WO 0053533 A1 WO0053533 A1 WO 0053533A1
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- reactor
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/06—Treatment of sludge; Devices therefor by oxidation
- C02F11/08—Wet air oxidation
- C02F11/086—Wet air oxidation in the supercritical state
-
- 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
- C02F2101/10—Inorganic compounds
Definitions
- the invention relates to a method for treating an aqueous waste stream containing salts according to the preamble of the first claim.
- an aqueous waste stream is to be understood as meaning saline wastewater contaminated with one or more organic pollutants, such as is produced, for example, as leachate in garbage and hazardous waste landfills or is released by the chemical or pharmaceutical industry.
- organic pollutants such as is produced, for example, as leachate in garbage and hazardous waste landfills or is released by the chemical or pharmaceutical industry.
- waste streams mainly contain chlorides and sulfates of sodium, potassium, calcium and magnesium as inorganic constituents.
- Organic constituents are usually dissolved or dispersed in a large number of organic pollutants, some of which are heteroatoms such as chlorine and / or other halides, sulfur and Contain phosphorus, such as chlorinated hydrocarbons, especially dioxins and furans.
- a method of the type mentioned is known from DE 31 18 348 C2. According to the process described there, a number of starting materials are converted into water under supercritical conditions in a reactor. For example, sea water or brine or other contaminated water containing organic materials is used. If the outlet temperature of the reactor is above 450 ° C, conventional ash separators can be used, which are connected downstream of the reactor and in which sodium chloride, calcium chloride, ferric oxide and the like are precipitated, so that a desalination effect is brought about (page 6, lines 23 ff.) . With this procedure, however, the problem arises that the salts at least partially precipitate out in the reactor and lead to blockages, because salts dissolve poorly in supercritical water. In addition, the oxidation of organic materials forms and the subsequent neutralization from existing heteroatoms additional salt, which increases the amount of precipitations.
- the problem of salt precipitation in the reactor can be mastered by setting the corresponding pressures and temperatures known from the publication by Bischoff and Pitzer, in particular if any necessary neutralization in the waste stream or hydrochloric acid formed by the reaction of organic chlorides is carried out only with sodium hydroxide solution or if the waste stream contains a high saline load.
- the salts of polyvalent metals, in particular calcium can only be kept in solution in supercritical water at uneconomically high pressures and temperatures.
- the salts of polyvalent metals therefore also precipitate out in a supercritical reactor if the pressure and temperature during the oxidation of the organic pollutants are set so that the precipitation of salts of monovalent metals, in particular sodium, is prevented. Since the precipitated salts accumulate in the reactor, the problem of clogging of pipelines and other components is only delayed and not prevented by such a procedure. On the other hand, for economic reasons, it is forbidden to withdraw the entire salt load from the waste stream before entering the reactor.
- the invention is therefore based on the object of preventing salt precipitation in the reactor during the oxidation of the organic pollutants of a salt-containing waste stream under supercritical conditions.
- the invention is based on the idea of separating only those salts before entering the reactor which cannot be kept in solution under the conditions prevailing in the reactor. These are the salts of polyvalent metals, especially calcium.
- the remaining salts are to be fed into the reactor with the waste stream, since they can be kept in solution under the pressures and temperatures known from Bischoff and Pitzer and therefore leave the reactor virtually completely. In this way the problem of precipitation in the reactor can be avoided.
- rature be chosen so that the dielectric constant of the water in the salt separator and the dielectric constant of the water in the reactor is up to 30% smaller; pressures and temperatures are particularly preferred at which the dielectric constant of the water in the salt separator corresponds to the dielectric constant of the water in the reactor or is slightly smaller, approximately up to 10%.
- the salt separator is preferably kept at a pressure of 200 to 800 bar and at a temperature of more than 100 ° C. If the pressure in the salt separator corresponds to the pressure in the reactor, this has the advantage that an additional pump for the salt separator can be dispensed with. However, the pressure in the salt separator can also be chosen lower; in this case the temperature in the salt separator is also reduced.
- the reactor is preferably operated at temperatures above 420 ° C., approximately between 420 ° C. and 600 ° C. and pressures above 350 bar, approximately between 350 and 800 bar.
- the temperatures and pressures are chosen depending on the concentration of the salts of monovalent metals, especially sodium. Under these conditions, the precipitation of salts of monovalent metals, especially sodium, in the Prevent the usual salt loads of the aqueous waste streams.
- the system described in the publication by Casal and Schmidt was used, which was supplemented by a thermal salt separator arranged upstream of the reactor.
- a simulated waste stream was passed through the salt separator and mixed with the oxidizing agent hydrogen peroxide before entering the reactor.
- the salt separator consisted of a pressure pipe, which was provided with an external heater. For heat recovery, the waste stream was conducted in countercurrent, so that it was cooled again when leaving the separator by the cooling effect of the waste stream introduced into the salt separator.
- aqueous solution was used to simulate the waste stream, in which chloride, sulfate, calcium and sodium were dissolved.
- concentrations of these ions are shown in the following table.
- the tests were carried out at an operating pressure of the salt separator of 250 bar and 500 bar.
- the inlet temperature of the simulated waste stream in the salt separator was in 20 ° C in both cases.
- the simulated waste stream was heated to 380 ° C in the salt separator.
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
Description
Verfahren zur Behandlung eines Salze enthaltenden wäßrigenProcess for treating an aqueous salt containing
AbfallStromsWaste streams
Die Erfindung betrifft ein Verfahren zur Behandlung eines Salze enthaltenden wäßrigen Abfallstroms gemäß dem Oberbegriff des ersten Patentanspruchs.The invention relates to a method for treating an aqueous waste stream containing salts according to the preamble of the first claim.
Unter einem wäßrigem Abfallstrom soll im folgenden salzhaltiges, mit einem oder mehreren organischen Schadstoffen verunreinigtes Abwasser verstanden werden, wie es beispielsweise als Sickerwasser in Müll- und Sondermülldeponien entsteht oder von der chemischen oder pharmazeutischen Industrie abgegeben wird. Solche Abfallströme enthalten als anorganische Bestandteile hauptsächlich Chloride und Sulfate von Natrium, Kalium, Calcium und Magnesium- Ais organische Bestandteile sind in der Regel eine Vielzahl organischer Schadstoffe gelöst oder dispergiert, die zum Teil He- teroatome wie Chlor und/oder andere Halogenide, Schwefel und Phosphor enthalten, wie zum Beispiel chlorierte Kohlenwasserstoffe, vor allem Dioxine und Furane .In the following, an aqueous waste stream is to be understood as meaning saline wastewater contaminated with one or more organic pollutants, such as is produced, for example, as leachate in garbage and hazardous waste landfills or is released by the chemical or pharmaceutical industry. Such waste streams mainly contain chlorides and sulfates of sodium, potassium, calcium and magnesium as inorganic constituents. Organic constituents are usually dissolved or dispersed in a large number of organic pollutants, some of which are heteroatoms such as chlorine and / or other halides, sulfur and Contain phosphorus, such as chlorinated hydrocarbons, especially dioxins and furans.
Ein Verfahren der eingangs genannten Art ist aus der DE 31 18 348 C2 bekannt. Gemäß dem dort beschriebenen Verfahren werden in einem Reaktor eine Reihe von Ausgangsstoffen unter überkritischen Bedingungen in Wasser umgesetzt. Beispielsweise wird Seewasser oder eine Sole oder ein anderes verunreinigtes Wasser eingesetzt, das organische Materialien enthält. Wenn die Auslaßtemperatur des Reaktors oberhalb 450°C liegt, können übliche Ascheabtrenner verwendet werden, die dem Reaktor nachgeschaltet sind und in denen Natriumchlorid, Kalziumchlorid, Ferrioxid und dergleichen ausgefällt werden, so daß ein Entsalzungseffekt bewirkt wird (Seite 6, Zeilen 23 ff.). Bei diesem Vorgehen tritt jedoch das Problem auf, daß die Salze zumindest teilweise bereits im Reaktor ausfallen und hier zu Verstopfungen führen, denn in überkritischem Wasser lösen sich Salze schlecht. Außerdem bildet sich bei der Oxidation der organischen Materialien und der anschließenden Neutralisation aus vorhandenen Heteroato- en zusätzliches Salz, das die Menge der Ausfällungen vergrößert .A method of the type mentioned is known from DE 31 18 348 C2. According to the process described there, a number of starting materials are converted into water under supercritical conditions in a reactor. For example, sea water or brine or other contaminated water containing organic materials is used. If the outlet temperature of the reactor is above 450 ° C, conventional ash separators can be used, which are connected downstream of the reactor and in which sodium chloride, calcium chloride, ferric oxide and the like are precipitated, so that a desalination effect is brought about (page 6, lines 23 ff.) . With this procedure, however, the problem arises that the salts at least partially precipitate out in the reactor and lead to blockages, because salts dissolve poorly in supercritical water. In addition, the oxidation of organic materials forms and the subsequent neutralization from existing heteroatoms additional salt, which increases the amount of precipitations.
Die Veröffentlichung von V. Casal und H. Schmidt: "SUWOX - a facility for the destruction of chlorinated hydrocarbons" im Journal of Supercritical Fluids 13 (1998) 269-276 beschreibt eine Anlage zur Oxidation von chlorierten Kohlenwasserstoffen in Wasser unter überkritischen Bedingungen, die bei Drücken von 400 bis 450 bar und Temperaturen von 420°C bis 500°C betrieben wird. Unter diesen Bedingungen kann Kochsalz, das durch Neutralisation mit Natronlauge aus der gebildeten Salzsäure entsteht, in Lösung gehalten werden.The publication by V. Casal and H. Schmidt: "SUWOX - a facility for the destruction of chlorinated hydrocarbons" in the Journal of Supercritical Fluids 13 (1998) 269-276 describes a plant for the oxidation of chlorinated hydrocarbons in water under supercritical conditions is operated at pressures from 400 to 450 bar and temperatures from 420 ° C to 500 ° C. Under these conditions, table salt, which is formed from the hydrochloric acid formed by neutralization with sodium hydroxide solution, can be kept in solution.
In der Veröffentlichung von James L. Bischoff und Kenneth S. Pitzer: "Liquid-Vapor Relations for the System NaCl-H20: Summary of the p-T-x Surface from 200° to 500°C", American Journal of Science, Vol. 289, March, 1989, pp . 217-248, ist die Abhängigkeit der Wasserlöslichkeit von Kochsalz in Abhängigkeit von Druck, Temperatur und Konzentration unter überkritischen Bedingungen in Diagrammen dargestellt. Aus den Diagrammen ergibt sich, daß sich bei einem Druck von 350 bar und einer Temperatur bis zu 420°C beträchtliche Mengen von Kochsalz in überkritischem Wasser lösen oder in Lösung bleiben; bei 750 bar können Temperaturen bis 550°C eingestellt werden, ohne daß Kochsalz ausfällt.In the publication by James L. Bischoff and Kenneth S. Pitzer: "Liquid-Vapor Relations for the System NaCl-H 2 0: Summary of the pTx Surface from 200 ° to 500 ° C", American Journal of Science, Vol. 289 , March, 1989, pp. 217-248, the dependence of the water solubility of table salt as a function of pressure, temperature and concentration is shown in diagrams under supercritical conditions. From the diagrams it follows that at a pressure of 350 bar and a temperature up to 420 ° C considerable amounts of table salt dissolve in supercritical water or remain in solution; At 750 bar, temperatures up to 550 ° C can be set without salt falling out.
Enthält der wäßrige Abfallstrom nur Kochsalz, kann das Problem der Salzausfällungen im Reaktor, wie in der Veröffentlichung von Casal und Schmidt beschrieben, dadurch beherrscht werden, daß die entsprechenden, aus der Veröffentlichung von Bischoff und Pitzer bekannten Drücke und Temperaturen eingestellt werden, insbesondere, wenn eine gegebenenfalls notwendige Neutralisation im Abfallstrom enthaltener oder durch Umsetzung von organischen Chloriden entstehender Salzsäure nur mit Natronlauge durchgeführt wird oder wenn der Abfallstrom eine hohe Kochsalzfracht enthält. Es hat sich jedoch gezeigt, daß die Salze mehrwertiger Metalle, insbesondere des Calciums, in überkritischem Wasser nur unter unwirtschaftlich hohen Drücken und Temperaturen in Lösung gehalten werden können. Die Salze mehrwertiger Metalle fallen daher in einem überkritischen Reaktor auch dann aus, wenn Druck und Temperatur bei der Oxidation der organischen Schadstoffe so eingestellt werden, daß die Ausfällung von Salzen einwertiger Metalle, insbesondere des Natriums, verhindert wird. Da sich die ausgefallenen Salze im Reaktor anreichern, wird das Problem des Verstopfens von Rohrleitungen und anderer Komponenten durch eine solche Verfahrensführung nur verzögert und nicht verhindert. Andererseits verbietet es sich aus wirtschaftlichen Gründen, dem Abfallstrom vor dem Eintritt in den Reaktor die gesamte Salzfracht zu entziehen.If the aqueous waste stream contains only common salt, the problem of salt precipitation in the reactor, as described in the publication by Casal and Schmidt, can be mastered by setting the corresponding pressures and temperatures known from the publication by Bischoff and Pitzer, in particular if any necessary neutralization in the waste stream or hydrochloric acid formed by the reaction of organic chlorides is carried out only with sodium hydroxide solution or if the waste stream contains a high saline load. However, it has been shown that the salts of polyvalent metals, in particular calcium, can only be kept in solution in supercritical water at uneconomically high pressures and temperatures. The salts of polyvalent metals therefore also precipitate out in a supercritical reactor if the pressure and temperature during the oxidation of the organic pollutants are set so that the precipitation of salts of monovalent metals, in particular sodium, is prevented. Since the precipitated salts accumulate in the reactor, the problem of clogging of pipelines and other components is only delayed and not prevented by such a procedure. On the other hand, for economic reasons, it is forbidden to withdraw the entire salt load from the waste stream before entering the reactor.
Der Erfindung liegt daher die Aufgabe zugrunde, Salzausfällungen im Reaktor während der Oxidation der organischen Schadstoffe eines salzhaltigen Abfallstroms unter überkritischen Bedingungen zu verhindern.The invention is therefore based on the object of preventing salt precipitation in the reactor during the oxidation of the organic pollutants of a salt-containing waste stream under supercritical conditions.
Die Lösung der Aufgabe ist im Kennzeichen des ersten Patentanspruchs beschrieben. Die weiteren Ansprüche geben bevorzugte Ausgestaltungen des Verfahrens an.The solution to the problem is described in the characterizing part of the first claim. The further claims indicate preferred embodiments of the method.
Der Erfindung liegt der Gedanke zugrunde, nur diejenigen Salze vor dem Eintritt in den Reaktor abzutrennen, die unter den im Reaktor herrschenden Bedingungen nicht in Lösung gehalten werden können. Dies sind die Salze mehrwertiger Metalle, insbesondere des Calciums. Die übrigen Salze sollen mit dem Abfallstrom in den Reaktor geleitet werden, da sie unter den durch Bischoff und Pitzer bekannten Drücken und Temperaturen in Lösung gehalten werden können und daher den Reaktor praktisch vollständig wieder verlassen. Auf diese Weise kann das Problem der Ausfällungen im Reaktor vermieden werden.The invention is based on the idea of separating only those salts before entering the reactor which cannot be kept in solution under the conditions prevailing in the reactor. These are the salts of polyvalent metals, especially calcium. The remaining salts are to be fed into the reactor with the waste stream, since they can be kept in solution under the pressures and temperatures known from Bischoff and Pitzer and therefore leave the reactor virtually completely. In this way the problem of precipitation in the reactor can be avoided.
Dies wird vorzugsweise dadurch erreicht, daß in einem dem Reaktor vorgeschalteten thermischen Salzabscheider Druck und Tempe- ratur so gewählt werden, daß die Dielektrizitätskonstante des Wassers im Salzabscheider der Dieelektrizitätskonstante des Wassers im Reaktor bis zu 30 % kleiner ist; besonders bevorzugt werden Drücke und Temperaturen, bei denen die Dielektrizitätskonstante des Wassers im Salzabscheider der Dieelektrizitätskonstante des Wassers im Reaktor entspricht oder geringfügig, etwa bis zu 10 %, kleiner ist. Der Salzabscheider wird vorzugsweise auf einem Druck von 200 bis 800 bar und bei einer Temperatur von mehr als 100°C gehalten. Entspricht der Druck im Salzabscheider dem Druck im Reaktor, hat dies den Vorteil, daß auf eine zusätzliche Pumpe für den Salzabscheider verzichtet werden kann. Der Druck im Salzabscheider kann jedoch auch niedriger gewählt werden; in diesem Fall wird auch die Temperatur im Salzabscheider vermindert .This is preferably achieved by pressure and temperature in a thermal salt separator upstream of the reactor. rature be chosen so that the dielectric constant of the water in the salt separator and the dielectric constant of the water in the reactor is up to 30% smaller; pressures and temperatures are particularly preferred at which the dielectric constant of the water in the salt separator corresponds to the dielectric constant of the water in the reactor or is slightly smaller, approximately up to 10%. The salt separator is preferably kept at a pressure of 200 to 800 bar and at a temperature of more than 100 ° C. If the pressure in the salt separator corresponds to the pressure in the reactor, this has the advantage that an additional pump for the salt separator can be dispensed with. However, the pressure in the salt separator can also be chosen lower; in this case the temperature in the salt separator is also reduced.
Es hat sich gezeigt, daß die Salze mehrwertiger Metalle, insbesondere des Calciums, häufig nicht erst unter überkritischen Bedingungen im Salzabscheider ausfallen, sondern bereits bei wesentlich tieferen Temperaturen, sofern im Salzabscheider ein Druck von 200 bis 700 bar aufrechterhalten wird. Es ist in diesen Fällen daher nicht unbedingt notwendig, auch den Salzabscheider unter überkritischen Bedingungen zu betreiben. Selbstverständlich können jedoch im Salzabscheider auch die im Reaktor eingestellten Drücke und Temperaturen eingestellt werden, wodurch ebenfalls eine praktisch vollständige Ausfällung von Calcium- und anderen Salzen mehrwertiger Metalle erzielt wird; allerdings ist eine solche Verfahrensführung weniger wirtschaftlich.It has been shown that the salts of polyvalent metals, in particular calcium, often do not precipitate in the salt separator only under supercritical conditions, but rather at much lower temperatures, provided that a pressure of 200 to 700 bar is maintained in the salt separator. In these cases it is therefore not absolutely necessary to operate the salt separator under supercritical conditions. However, the pressures and temperatures set in the reactor can of course also be set in the salt separator, as a result of which virtually complete precipitation of calcium and other salts of polyvalent metals is also achieved; however, such a process is less economical.
Der Reaktor wird vorzugsweise bei Temperaturen oberhalb von 420°C, etwa zwischen 420°C und 600°C und Drücken oberhalb von 350 bar, etwa zwischen 350 und 800 bar, betrieben. Die Temperaturen und Drücke werden in Abhängigkeit von der Konzentration der Salze einwertiger Metalle, insbesondere des Natriums, gewählt. Unter diesen Bedingungen läßt sich die Ausfällung von Salzen einwertiger Metalle, insbesondere des Natriums, bei den üblichen Salzfrachten der wäßrigen Abfallströme sicher verhindern.The reactor is preferably operated at temperatures above 420 ° C., approximately between 420 ° C. and 600 ° C. and pressures above 350 bar, approximately between 350 and 800 bar. The temperatures and pressures are chosen depending on the concentration of the salts of monovalent metals, especially sodium. Under these conditions, the precipitation of salts of monovalent metals, especially sodium, in the Prevent the usual salt loads of the aqueous waste streams.
Das bei der Oxidation von organischen Schadstoffen mit Heteroa- tomen auftretende Korrosionsproblem, das auf die Bildung sehr aggressiver Säuren wie z. B. Chlorwasserstoff, Schwefelsäure, Salpetersäure und Flußsäure zurückzuführen ist, kann einerseits in bekannter Weise durch Neutralisation mit Natronlauge gelöst werden. Andererseits kann das Korrosionsproblem im Reaktor durch korrosionsresistente Reaktoreinbauten, etwa aus Titan oder aus einer Keramik wie z. B. Aluminiumoxid oder Siliciumcarbid, beherrscht werden.The corrosion problem that occurs in the oxidation of organic pollutants with heteroatoms, which is due to the formation of very aggressive acids such as. B. hydrogen chloride, sulfuric acid, nitric acid and hydrofluoric acid can be solved on the one hand in a known manner by neutralization with sodium hydroxide solution. On the other hand, the corrosion problem in the reactor through corrosion-resistant reactor internals, such as titanium or a ceramic such as. As aluminum oxide or silicon carbide, are mastered.
Die Erfindung wird im folgenden anhand von Ausführungsbeispielen näher erläutert.The invention is explained in more detail below on the basis of exemplary embodiments.
Zur Durchführung der Beispiele wurde die in der Veröffentlichung von Casal und Schmidt beschriebene Anlage eingesetzt, die durch einen in Strömungsrichtung vor dem Reaktor angeordneten thermischen Salzabscheider ergänzt wurde. Ein simulierter Abfallstrom wurde durch den Salzabscheider geleitet und vor dem Eintritt in den Reaktor mit dem Oxidations ittel Wasserstoffperoxid vermischt. Der Salzabscheider bestand aus einem Druckrohr, das mit einer außen angebrachte Heizung versehen war. Zur Wärmerückgewinnung wurde der Abfallstrom im Gegenstrom geführt, so daß er beim Verlassen des Abscheiders durch die Kühlwirkung des in den Salzabscheider eingeleiteten Abfallstroms wieder abgekühlt wurde .To carry out the examples, the system described in the publication by Casal and Schmidt was used, which was supplemented by a thermal salt separator arranged upstream of the reactor. A simulated waste stream was passed through the salt separator and mixed with the oxidizing agent hydrogen peroxide before entering the reactor. The salt separator consisted of a pressure pipe, which was provided with an external heater. For heat recovery, the waste stream was conducted in countercurrent, so that it was cooled again when leaving the separator by the cooling effect of the waste stream introduced into the salt separator.
Um die Wirkung des Salzabscheiders zu demonstrieren, wurde zur Simulation des Abfallstroms eine wäßrige Lösung eingesetzt, in der Chlorid, Sulfat, Calcium und Natrium gelöst waren. Die Konzentrationen dieser Ionen geht aus der folgenden Tabelle hervor. Die Versuche wurden bei einem Betriebsdruck des Salzabscheiders von 250 bar und 500 bar durchgeführt. Die Eintrittstemperatur des simulierten Abfallstroms in den Salzabscheider betrug in beiden Fällen 20°C. Im Salzabscheider wurde der simulierte Abfallstrom auf 380°C erhitzt.To demonstrate the effect of the salt separator, an aqueous solution was used to simulate the waste stream, in which chloride, sulfate, calcium and sodium were dissolved. The concentrations of these ions are shown in the following table. The tests were carried out at an operating pressure of the salt separator of 250 bar and 500 bar. The inlet temperature of the simulated waste stream in the salt separator was in 20 ° C in both cases. The simulated waste stream was heated to 380 ° C in the salt separator.
Tabelletable
BetriebsIonen Eintrag in den Austrag aus dem bedingungen Salzabscheider SalzabscheiderOperating ion entry in the discharge from the salt separator conditions
[mg/1] [mg/1] p = 250 bar Chlorid 2100 2077[mg / 1] [mg / 1] p = 250 bar chloride 2100 2077
Sulfat 2140 1076Sulfate 2140 1076
Calcium 404 5,3Calcium 404 5.3
Natrium 1920 1916 p = 500 bar Chlorid 2100 2099Sodium 1920 1916 p = 500 bar chloride 2100 2099
Sulfat 2140 1202Sulfate 2140 1202
Calcium 404 10,2Calcium 404 10.2
Natrium 1920 1932Sodium 1920 1932
Wie sich aus der Tabelle ergibt, konnten in dem Salzabscheider bei 250 bar nahezu 99 % und bei 500 bar über 97 % des Calciums zurückgehalten werden, während innerhalb der Meßgenauigkeit eine Abscheidung von Natrium nicht erkennbar war. Ebenso wie Natrium wird auch Chlorid im Salzabscheider praktisch nicht zurückgehalten, während Sulfat etwa zur Hälfte abgeschieden wird. As can be seen from the table, almost 99% of the calcium could be retained in the salt separator at 250 bar and more than 97% of the calcium at 500 bar, while a deposition of sodium was not discernible within the measuring accuracy. Like sodium, chloride is practically not retained in the salt separator, while about half of the sulfate is separated out.
Claims
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE1999110211 DE19910211C2 (en) | 1999-03-09 | 1999-03-09 | Process for treating an aqueous waste stream containing salts |
| DE19910211.2 | 1999-03-09 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| WO2000053533A1 true WO2000053533A1 (en) | 2000-09-14 |
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| Application Number | Title | Priority Date | Filing Date |
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| PCT/EP2000/001544 Ceased WO2000053533A1 (en) | 1999-03-09 | 2000-02-25 | Method for treating an aqueous waste stream containing salts |
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| DE (1) | DE19910211C2 (en) |
| WO (1) | WO2000053533A1 (en) |
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| NL1035729C2 (en) * | 2008-07-21 | 2010-01-22 | Stichting Wetsus Ct Of Excelle | Method and system for supercritical removal or an inorganic compound. |
| DE102008053618A1 (en) * | 2008-10-29 | 2010-07-01 | Karlsruher Institut für Technologie | Process for the precipitation of salts |
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|---|---|---|---|---|
| US4543190A (en) * | 1980-05-08 | 1985-09-24 | Modar, Inc. | Processing methods for the oxidation of organics in supercritical water |
| US4822497A (en) * | 1987-09-22 | 1989-04-18 | Modar, Inc. | Method for solids separation in a wet oxidation type process |
| US4891140A (en) * | 1989-01-09 | 1990-01-02 | Burke Jr Jerry A | Desalination process |
| WO1991011394A1 (en) * | 1990-01-31 | 1991-08-08 | Modar, Inc. | Process for oxidation of materials in water at supercritical temperatures |
| US5252224A (en) * | 1991-06-28 | 1993-10-12 | Modell Development Corporation | Supercritical water oxidation process of organics with inorganics |
| US5543057A (en) * | 1995-03-13 | 1996-08-06 | Abitibi-Price, Inc. | Supercritical water oxidation of organics using a mobile surface |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL90468C (en) * | 1955-02-09 | 1900-01-01 | ||
| US6103129A (en) * | 1994-01-14 | 2000-08-15 | 3500764 Canada Inc. | Method for the critical water oxidation of organic compounds |
| US6017460A (en) * | 1996-06-07 | 2000-01-25 | Chematur Engineering Ab | Heating and reaction system and method using recycle reactor |
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1999
- 1999-03-09 DE DE1999110211 patent/DE19910211C2/en not_active Expired - Fee Related
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2000
- 2000-02-25 WO PCT/EP2000/001544 patent/WO2000053533A1/en not_active Ceased
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4543190A (en) * | 1980-05-08 | 1985-09-24 | Modar, Inc. | Processing methods for the oxidation of organics in supercritical water |
| US4822497A (en) * | 1987-09-22 | 1989-04-18 | Modar, Inc. | Method for solids separation in a wet oxidation type process |
| US4891140A (en) * | 1989-01-09 | 1990-01-02 | Burke Jr Jerry A | Desalination process |
| WO1991011394A1 (en) * | 1990-01-31 | 1991-08-08 | Modar, Inc. | Process for oxidation of materials in water at supercritical temperatures |
| US5252224A (en) * | 1991-06-28 | 1993-10-12 | Modell Development Corporation | Supercritical water oxidation process of organics with inorganics |
| US5543057A (en) * | 1995-03-13 | 1996-08-06 | Abitibi-Price, Inc. | Supercritical water oxidation of organics using a mobile surface |
Also Published As
| Publication number | Publication date |
|---|---|
| DE19910211C2 (en) | 2001-02-22 |
| DE19910211A1 (en) | 2000-09-21 |
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