Wet oxidation method

Description

[0001] The present invention relates to a new wet oxidation method.

[0002] Wet oxidation, also known as wet-phase oxidation, is an autocatalytic process that breaks down by oxidation organic or inorganic substances that are present in a liquid phase (aqueous solutions or suspensions) by using oxygen dissolved directly in said liquid phase.

[0003] The concentration of oxidizable species can be expressed as C.O.D. (cumulative oxygen demand), which expresses the amount of oxygen in mg/l or kg/m³ of water required for complete breakdown of the substances that are present.

[0004] The wet oxidation process is in itself exothermic, but to work in industrially acceptable times it is usually necessary to heat the wastewater to a temperature (generally 200-250 °C) at which the oxygen has a sufficiently high reactivity with respect to the sewage. When working at this temperature, however, it is necessary to apply intense pressures in order to keep the water in the liquid state.

[0005] At the same time, there is also a maximum temperature (generally 300-320 °C, depending on the type of pollutants) that the wastewater cannot exceed. This limit arises from the fact that the maximum amount of heat that can be accumulated in the reaction water and in the gaseous phase that accompanies it (heat generated by the oxidation of the pollutants) is limited by the maximum operating temperature of the reactor and in any case cannot exceed 374 °C, the temperature at which liquid water can no longer exist.

[0006] This factor is a particularly strong limitation when working with pure oxygen or oxygen-enriched air, since the limited amount of gaseous phase that is present in the reactor limits the evaporation of the water and the consequent absorption of the corresponding latent heat of evaporation. Accordingly, current processes, in order to operate safely, require the amount of pollutants treated per time unit and of introduced oxygen to not exceed certain levels set by the nature of the reaction and most of all by the practical method with which the wet oxidation is performed.

[0007] With temperatures of the input wastewater of approximately 200-270 °C and output temperatures of approximately 300-320 °C, the maximum amount of oxygen that can be introduced (and therefore consumed) does not exceed 20-50 kg per cubic meter of water, whereas it would be instead highly desirable to be able to work at higher oxygen concentrations, so as to reduce the volumes of gas that pass through the reactor and have a higher amount of oxygen dissolved in the sewage (a quantity that depends on pO₂).

[0008] USP 4,869,833 discloses a method for wet oxidation of materials in waste streams, comprising the introduction of a waste stream or first reactant with a second reactant through a tubular coil.

[0009] Accordingly, the aim of the invention is to provide a process for the wet oxidation of one or more organic and inorganic substances that overcomes the drawbacks of the background art.

[0010] Within this aim, one of the objects is to provide a wet oxidation process that allows to increase the C.O.D. processed per time unit without varying the internal dimensions, temperature and pressure of the reactor.

[0011] Another object is to provide a wet oxidation process as described above that allows to treat simultaneously pollutants characterized by a highly different oxidation potential.

[0012] This aim and these and other objects are achieved by a method for wet oxidation of one or more oxidizable compounds, said method comprising the step of introducing in a wet oxidation apparatus at least two wastewaters that are mutually different at least in terms of input temperature and C.O.D.

[0013] Further characteristics and advantages of the present invention will become better apparent from the description of some preferred but not exclusive embodiments thereof, wherein:

Figure 1 is a block diagram that describes a method according to the invention, performed with the aid of an apparatus constituted by an individual reactor that operates continuously and in which a second wastewater, characterized by a high C.O.D. and by a lower temperature than the wastewater added at the input of said reactor, is added in a point that lies above the base;

Figure 2 is a block diagram that describes a method according to the invention, performed with the aid of an apparatus constituted by two reactors that operate in series and continuously, wherein the addition of a first wastewater at the input of the apparatus is followed by the addition, between the two reactors, of a second wastewater that is characterized by a high C.O.D. and by a lower temperature than the first wastewater.

[0014] The expression "oxidizable compound" is preferably used to designate any complex organic or inorganic compound that is present in the wastewaters to be treated and often has a high environmental toxicity. The oxidizable compound is advantageously degraded as a consequence of the oxidation of its structure, where said breakdown of the compound consists for example in breaking up the initial complex structure into structurally simpler fragments characterized by lower environmental toxicity. Degradation does not necessarily have to attain complete transformation of the compound into simple products such as carbon dioxide, water, molecular nitrogen, metallic oxides, nitrogen oxides or sulfur oxides and others.

[0015] The term "apparatus" is used to designate a plant for performing a wet oxidation process, preferably the reactor or set of reactors inside which the oxidation occurs physically. The term "reactors" includes both reactors that operate continuously and reactors that operate in batch mode. When working with multiple reactors connected in series, the term "apparatus" also designates the means and parts of the plant that connect the individual reactors. This also comprises the devices required to perform the process, such as heat exchangers, wastewater collection tanks, pumps for feeding the wastewater under pressure and for modifying the operating pressure inside the reactor.

[0016] The term "wastewater" is used to designate any reagent of a conventional wet oxidation process. For example, a wastewater is an aqueous mixture of one or more organic and/or inorganic pollutants (oxidizable compounds as defined above). The wastewater can be in any physical form, advantageously an aqueous solution and/or suspension. Moreover, the invention allows to treat both monostream and multistream wastewaters, where the term "monostream" is used to designate wastewater comprising a single type of pollutant, whereas "multistream" is used to designate wastewater comprising various types of pollutants. Moreover, wastewaters according to the invention can comprise both oxidizable and non-oxidizable substances, wherein only the former are of course attacked by the oxygen.

[0017] The expression "input temperature" is used to designate the temperature of the wastewater when it is introduced in the apparatus.

[0018] The C.O.D. indirectly expresses the amount of heat that can be generated by a unit mass of the wastewater to which reference is made, since it includes the concentration and degree of oxidizability of the pollutants that are present. In other words, the C.O.D. describes the characteristics and concentration of the pollutants regardless of their chemical nature, their reactivity to oxidation and the enthalpic gain that arises from their complete oxidation.

[0019] In a first aspect, the invention relates to a method for wet oxidation of one or more oxidizable, organic and/or inorganic substances, the method comprising the step of introducing into an apparatus for carrying out said method, at least two wastewaters wherein when they are introduced said wastewaters have mutually different temperatures and C.O.D. and wherein the wastewater having having a lower temperature has a higher C.O.D. and viceversa.

[0020] Although it is preferable to introduce in the apparatus only two wastewaters, it is possible to process simultaneously even more than two, on condition that within the pool of wastewaters that are introduced, at least two of them have mutually different input temperatures and C.O.D. values.

[0021] The wastewater input points are preferably "dedicated" in terms of temperature and C.O.D., in that an input point corresponds to the addition of a type of wastewater, be it a monostream or a multistream, that is characterized by a specific temperature/C.O.D. ratio. Particularly advantageously, and considering the preferred case in which there are only two wastewaters, the wastewater fed at the higher temperature has a lower C.O.D. and is introduced in a point that lies closer to the input of the apparatus with respect to the feed of the colder wastewater, which has the higher C.O.D. Preferably, the input point of the wastewater at the higher temperature coincides with the input of the apparatus, which can be the base of the first or only reactor.

[0022] In the particularly preferred case in which there are two input wastewaters, the wastewater at the higher temperature preferably has an input temperature comprised between 160 °C and 300 °C, even more preferably comprised between 200 °C and 280 °C, while the second (colder) wastewater preferably has an input temperature comprised between 10 °C and 160 °C, advantageously equal to approximately 25 °C. Regardless of the number of input wastewaters, it is advantageous for at least one wastewater to have an input temperature comprised between 200 °C and 280 °C.

[0023] In the particularly preferred case in which there are two input wastewaters, the wastewater at the higher temperature has a C.O.D. comprised between 10000 mg/l and 75000 mg/l, while the wastewater at the lower temperature has a C.O.D. comprised between 75000 mg/l and 300000 mg/l.

[0024] It can be appreciated, therefore, that the method according to the invention allows to process wastewaters with a C.O.D. up to 300000 mg/l, while the background art generally cannot exceed C.O.D. values of 75000 mg/l.

[0025] In the particularly preferred case in which there are two input wastewaters, the volume of the wastewater having the lower temperature is comprised between 2.5% and 35% of the wastewater input earlier.

[0026] According to another embodiment of the invention, multiple wastewaters are introduced at gradually increasing heights from the bottom of the apparatus, so that the wastewater added in an upward position utilizes, in order to be heated, the heat generated by the oxidation of the wastewaters introduced in points that lie below it. A greater distance from the input of the apparatus is matched by a lower temperature and a higher C.O.D.

[0027] The method according to the invention can occur equally in a continuous mode or in batch mode, in multiple reactors continuously or in a single reactor. If the method occurs continuously in multiple reactors connected in series, the addition of wastewaters at a lower temperature is performed advantageously after the first reactor. If the method is performed in batch mode, the addition of the second wastewater or of the additional wastewaters does not occur simultaneously with the introduction of the first wastewater. In particular, the subsequent addition or additions is, or are, preferably performed after a time interval typically comprised between 10 and 60 minutes, so that the mixture inside the reactor can reach a level (typically a temperature comprised between 160 °C and 300 °C) high enough to allow the continuation of the oxidation reaction.

[0028] With respect to conventional methods and for equal operating conditions and apparatus characteristics, the method according to the invention allows to achieve the significant advantage of increasing considerably the amount of oxygen consumed, with the consequence of increasing the amount of pollutants that can be oxidized per time unit.

[0029] One of the fundamental differences between conventional wet oxidation processes and the method according to the invention therefore resides in the combined treatment of a first wastewater characterized by a conventional C.O.D., introduced for example at the base of the reactor advantageously after a preliminary heating step, and of at least one second wastewater, introduced in a point that lies further from the input point of the first wastewater and, with respect to the first wastewater, is characterized by a lower temperature and a higher C.O.D. It is believed that the first wastewater transfers part of the energy stored therein to the second wastewater, so as to bring it to a temperature at which the oxidation reaction can assume a rate that is compatible with an industrial process. The second wastewater (i.e., the wastewater at a lower temperature), however, has a higher C.O.D., and therefore oxidation resumes without altering the thermal balance of the reaction (i.e., the temperature differential between the input point and the output point of the apparatus remains constant). In other words, the heat generated by the oxidation of a wastewater that has a particularly high C.O.D. but is fed at a low temperature compensates for the heat transferred to it by the first wastewater, so as to keep the average temperature of the apparatus at a level that is compatible with swift and regular oxidation of the pollutants and most of all so as to maintain a temperature gradient that is optimized beforehand so as to provide the best oxidation yields. In the background art, treatment of wastewaters with particularly high C.O.D. values was difficult to perform and in any case impossible with conventional methods, as it would have required a considerable dilution of the wastewater. On the basis of what has been described, once the wastewater input points have been set, the higher the C.O,D. delta, the higher the temperature delta must be.

[0030] The person skilled in the art will easily understand that the advantages described, which arise from the input of a cold and concentrated wastewater, can be applied to many other situations that have not been specified explicitly. For example, it is possible to add, at a same input level (distance from the base of the reactor), two or more wastewaters having a different C.O.D., calculating their input temperatures so as to keep the total temperature differential between the base and the apex of the apparatus unchanged.

[0031] In a preferred embodiment, at least one wastewater is introduced at the base of the wet oxidation apparatus and is brought beforehand to the temperature at which the oxidation reaction is triggered by means of a preheating step, so that it supplies heat to the wastewaters introduced subsequently, which are colder, advantageously at ambient temperature.

[0032] It is also possible to preheat more than one single wastewater, wherein each wastewater is brought to a different temperature and accordingly is introduced in the apparatus at a different height from the input point.

[0033] Further characteristics and advantages of the present invention will become better apparent from the description of the following preferred embodiments, intended exclusively by way of non-limiting example.

Example 1

[0034] A partial wet oxidation apparatus, in which wastewater of a chemical factory and various aqueous wastes originating externally are treated which are characterized by the following parameters: a) C.O.D. 20000-50000 mg/l, b) chlorides: 20000-50000 mg/l (as Cl^-), c) sulphates: 5000-20000 mg/l (as SO₄^2-) , d) suspended solids: 1000-15000 mg/l.

[0035] The reaction parameters are: temperature: 250-310 °C; pressure: 110-150 bars.

[0036] The apparatus works with three reactors in series, each having an inside diameter of approximately 0.75 meters and a height of approximately 9 meters.

[0037] During normal operation, the first reactor was supplied with wastewater with a C.O.D. of 40000 mg/l at a flow-rate of 12 m³/h (equal to approximately 12600 kg/h) and oxygen in a stoichiometric quantity (480 kg/h) at a temperature of 250 °C. The reaction proceeded regularly with a temperature gradient of approximately 50 °C (output temperature from the fourth reactor equal to approximately 300 °C) and conversion (C.O.D. reduction) of more than 75%. The output temperature from the first reactor was approximately 265 °C.

[0038] 1.2 m³/h of a wastewater with a high C.O.D. (160000 mg/l) at ambient temperature (approximately 25 °C) were then added in the second reactor, simultaneously increasing the amount of oxygen fed (up to 670 kg/h) so as to keep the stoichiometric ratio between oxygen and C.O.D. constant.

[0039] Due to the addition of the cold wastewater, the bottom temperature of the second reactor decreased to approximately 245 °C (from the initial 265 ° C), but due to the higher reaction heat generated as a consequence of the addition of C.O.D. the output temperature from the fourth reactor remained practically unchanged.

[0040] Although in the text only some embodiments of the invention have been described, the person skilled in the art will understand immediately that the invention, in all of its aspects, is susceptible of variations and modifications, all of which are within the scope of the appended claims and are adapted to obtain other equally advantageous embodiments.

[0041] The disclosures in Italian Patent Application No. MI2004A001239 from which this application claims priority are incorporated herein by reference.

[0042] Where technical features mentioned in any claim are followed by reference signs, those reference signs have been included for the sole purpose of increasing the intelligibility of the claims and accordingly, such reference signs do not have any limiting effect on the interpretation of each element identified by way of example by such reference signs.

Claims

1. A method for the wet oxidation of one or more oxidizable compounds, characterized in that it comprises the step of introducing, in a wet oxidation apparatus, at least two wastewaters that are mutually different at least in terms of input temperature and Cumulative Oxygen Demand (C.O.D.), which expresses the amount of oxygen in mg/l or kg/m³ of water required for complete breakdown of the substances that are present.

2. The method according to claim 1, characterized in that the wastewaters are aqueous solutions or suspensions.

3. The method according to claim 1, characterized in that the wastewaters are monostream or multistream.

4. The method according to claim 1, characterized in that the input wastewaters are two.

5. The method according to claim 1, characterized in that the wastewater having the higher C.O.D. has a lower temperature than the other wastewater.

6. The method according to claim 1, characterized in that the wastewater having the lower C.O.D. is introduced in a point that is closer to the inlet of the apparatus with respect to the wastewater having a higher C.O.D.

7. The method according to claim 6, characterized in that the wastewater having the lower C.O.D. is introduced at the inlet of the apparatus.

8. The method according to claim 1, characterized in that the wastewater having a higher temperature has an input temperature comprised between 160 °C and 300 °C, even more preferably comprised between 200 °C and 280 °C.

9. The method according to claim 1, characterized in that the wastewater having the lower temperature has an input temperature comprised between 10 °C and 160 °C, advantageously equal to 25°C.

10. The method according to claim 1, characterized in that the wastewater having the higher temperature has a C.O.D. comprised between 10000 mg/l and 75000 mg/l.

11. The method according to claim 1, characterized in that the wastewater having the lower temperature has a C.O.D. comprised between 75000 mg/l and 300000 mg/l.

12. The method according to claim 1, characterized in that the introduced volume of wastewater having the higher C.O.D. is comprised between 2.5 and 35% of the wastewater having the lower C.O.D.

Ansprüche

1. Ein Verfahren zur Nassoxidation einer oder mehrerer oxidierbarer Verbindungen, dadurch gekennzeichnet, dass es den Schritt des Einführens mindestens zweier Abwässer umfasst, die sich mindestens im Hinblick auf Eingangstemperatur und kumulativen Sauerstoffbedarf (Cumulative Oxygen Demand, C.O.D.) unterscheiden, der die Menge an Sauerstoff in mg/l oder kg/m³ von Wasser exprimiert, die für einen kompletten Abbau der Substanzen erforderlich ist, die vorhanden sind.

2. Das Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass die Abwässer wässerige Lösungen oder Suspensionen sind.

3. Das Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass die Abwässer einströmig oder mehrströmig sind.

4. Das Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass es zwei Eingangs-Abwässer gibt.

5. Das Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass das Abwasser mit dem höheren C.O.D. eine niedrigere Temperatur hat als das andere Abwasser.

6. Das Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass das Abwasser mit dem niedrigeren C.O.D. an einem Punkt eingeführt wird, der näher am Einlass der Vorrichtung liegt als das Abwasser mit dem höheren C.O.D.

7. Das Verfahren gemäß Anspruch 6, dadurch gekennzeichnet, dass das Abwasser mit dem niedrigeren C.O.D. am Einlass der Vorrichtung eingeführt wird.

8. Das Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass das Abwasser mit der höheren Temperatur eine Eingangstemperatur zwischen 160°C und 300°C, noch stärker bevorzugt zwischen 200°C und 280°C, hat.

9. Das Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass das Abwasser mit der niedrigeren Temperatur eine Eingangstemperatur zwischen 10°C und 160°C, praktischerweise gleich 25°C, hat.

10. Das Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass das Abwasser mit der höheren Temperatur einen C.O.D. zwischen 10000 mg/l und 75000 mg/l hat.

11. Das Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass das Abwasser mit der niedrigeren Temperatur einen C.O.D. zwischen 75000 mg/l und 300000 mg/l hat.

12. Das Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass das eingeführte Volumen von Abwasser mit dem höheren C.O.D. zwischen 2,5 und 35% des Abwassers mit dem niedrigeren C.O.D. beträgt.

Revendications

1. Procédé pour l'oxydation par voie humide d'un ou plusieurs composants oxydables, caractérisé en ce qu'il comprend l'étape consistant à introduire, dans un appareil pour l'oxydation par voie humide, au moins deux eaux usées qui sont mutuellement différentes au moins en terme de température d'entrée et de Demande Cumulative d'Oxygène (D.C.O.), qui exprime le montant d'oxygène en mg/l ou en kg/m³ d'eau requise pour la cassure complète des substances qui sont présentes.

2. Procédé selon la revendication 1, caractérisé en ce que les eaux usées sont des solutions ou des suspensions aqueuses.

3. Procédé selon la revendication 1, caractérisé en ce que les eaux usées sont à courant unique ou à courants multiples.

4. Procédé selon la revendication 1, caractérisé en ce que les eaux usées en entrée sont deux.

5. Procédé selon la revendication 1, caractérisé en ce que l'eau usée présentant la D.C.O. la plus élevée présente une température plus basse que l'autre eau usée.

6. Procédé selon la revendication 1, caractérisé en ce que l'eau usée présentant la D.C.O. la plus basse est introduite dans un point qui est plus proche de l'entrée de l'appareil par rapport à l'eau usée présentant une D.C.O. plus élevée.

7. Procédé selon la revendication 6, caractérisé en ce que l'eau usée présentant la D.C.O. la plus basse est introduite au niveau de l'entrée de l'appareil.

8. Procédé selon la revendication 1, caractérisé en ce que l'eau usée présentant une température plus élevée présente une température d'entrée comprise entre 160° C et 300° C, même plus préférablement comprise entre 200° C et 280° C.

9. Procédé selon la revendication 1, caractérisé en ce que l'eau usée présentant la température la plus basse présente une température d'entrée comprise entre 10° C et 160° C, avantageusement égale à 25° C.

10. Procédé selon la revendication 1, caractérisé en ce que l'eau usée présentant la température la plus élevée présente une D.C.O. comprise entre 10000 mg/l et 75000 mg/l.

11. Procédé selon la revendication 1, caractérisé en ce que l'eau usée présentant la température la plus basse présente une D.C.O. comprise entre 75000 mg/l et 300000 mg/l.

12. Procédé selon la revendication 1, caractérisé en ce que le volume introduit d'eau usée présentant la D.C.O. la plus élevée est compris entre 2,5 et 35% de l'eau usée présentant la D.C.O. la plus basse.

Drawing