ES2265728B1 - SYSTEM FOR THE ELIMINATION OF ORGANIC MICROCONTAMINANTS IN THE WATER THROUGH THE USE OF OZONE AND ACTIVATED CARBON. - Google Patents
SYSTEM FOR THE ELIMINATION OF ORGANIC MICROCONTAMINANTS IN THE WATER THROUGH THE USE OF OZONE AND ACTIVATED CARBON. Download PDFInfo
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- ES2265728B1 ES2265728B1 ES200402217A ES200402217A ES2265728B1 ES 2265728 B1 ES2265728 B1 ES 2265728B1 ES 200402217 A ES200402217 A ES 200402217A ES 200402217 A ES200402217 A ES 200402217A ES 2265728 B1 ES2265728 B1 ES 2265728B1
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 78
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 34
- 238000003379 elimination reaction Methods 0.000 title claims abstract description 13
- 230000008030 elimination Effects 0.000 title claims abstract description 12
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 58
- 238000011282 treatment Methods 0.000 claims abstract description 35
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 10
- 239000008346 aqueous phase Substances 0.000 claims abstract description 7
- 239000012071 phase Substances 0.000 claims abstract description 6
- 230000002572 peristaltic effect Effects 0.000 claims abstract description 3
- 238000000034 method Methods 0.000 claims description 29
- 230000008569 process Effects 0.000 claims description 28
- 238000006385 ozonation reaction Methods 0.000 claims description 22
- 239000003643 water by type Substances 0.000 claims description 9
- 239000003054 catalyst Substances 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 3
- 238000005119 centrifugation Methods 0.000 claims description 2
- 238000005189 flocculation Methods 0.000 claims description 2
- 230000016615 flocculation Effects 0.000 claims description 2
- 239000012528 membrane Substances 0.000 claims description 2
- 239000000843 powder Substances 0.000 claims description 2
- 238000001556 precipitation Methods 0.000 claims description 2
- 238000000746 purification Methods 0.000 abstract description 17
- 231100000331 toxic Toxicity 0.000 abstract description 5
- 230000002588 toxic effect Effects 0.000 abstract description 5
- 239000003651 drinking water Substances 0.000 abstract description 4
- 235000020188 drinking water Nutrition 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 3
- 238000005191 phase separation Methods 0.000 abstract description 3
- GVGUFUZHNYFZLC-UHFFFAOYSA-N dodecyl benzenesulfonate;sodium Chemical compound [Na].CCCCCCCCCCCCOS(=O)(=O)C1=CC=CC=C1 GVGUFUZHNYFZLC-UHFFFAOYSA-N 0.000 description 24
- 229940080264 sodium dodecylbenzenesulfonate Drugs 0.000 description 24
- 230000003197 catalytic effect Effects 0.000 description 9
- 230000003647 oxidation Effects 0.000 description 9
- 238000007254 oxidation reaction Methods 0.000 description 9
- 150000001875 compounds Chemical class 0.000 description 7
- 230000015556 catabolic process Effects 0.000 description 6
- 238000006731 degradation reaction Methods 0.000 description 6
- 230000009466 transformation Effects 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 238000001179 sorption measurement Methods 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 230000001590 oxidative effect Effects 0.000 description 4
- 231100000419 toxicity Toxicity 0.000 description 4
- 230000001988 toxicity Effects 0.000 description 4
- 230000001131 transforming effect Effects 0.000 description 4
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 description 3
- 239000005446 dissolved organic matter Substances 0.000 description 3
- ZPBSAMLXSQCSOX-UHFFFAOYSA-N naphthalene-1,3,6-trisulfonic acid Chemical compound OS(=O)(=O)C1=CC(S(O)(=O)=O)=CC2=CC(S(=O)(=O)O)=CC=C21 ZPBSAMLXSQCSOX-UHFFFAOYSA-N 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 230000009257 reactivity Effects 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 230000000274 adsorptive effect Effects 0.000 description 2
- 238000009303 advanced oxidation process reaction Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000004042 decolorization Methods 0.000 description 2
- 230000002708 enhancing effect Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 230000036541 health Effects 0.000 description 2
- 231100000086 high toxicity Toxicity 0.000 description 2
- 239000003295 industrial effluent Substances 0.000 description 2
- 239000003999 initiator Substances 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- LPXPTNMVRIOKMN-UHFFFAOYSA-M sodium nitrite Chemical compound [Na+].[O-]N=O LPXPTNMVRIOKMN-UHFFFAOYSA-M 0.000 description 2
- 239000007858 starting material Substances 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical class OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- FBPFZTCFMRRESA-NQAPHZHOSA-N Sorbitol Chemical compound OCC(O)[C@H](O)[C@@H](O)[C@H](O)CO FBPFZTCFMRRESA-NQAPHZHOSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 150000001450 anions Chemical group 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000000982 direct dye Substances 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000001738 genotoxic effect Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 238000000265 homogenisation Methods 0.000 description 1
- XMBWDFGMSWQBCA-UHFFFAOYSA-N hydrogen iodide Chemical compound I XMBWDFGMSWQBCA-UHFFFAOYSA-N 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- PSZYNBSKGUBXEH-UHFFFAOYSA-N naphthalene-1-sulfonic acid Chemical class C1=CC=C2C(S(=O)(=O)O)=CC=CC2=C1 PSZYNBSKGUBXEH-UHFFFAOYSA-N 0.000 description 1
- 150000004045 organic chlorine compounds Chemical class 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 235000006408 oxalic acid Nutrition 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000003415 peat Substances 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 230000035945 sensitivity Effects 0.000 description 1
- 235000010288 sodium nitrite Nutrition 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 235000010356 sorbitol Nutrition 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- 239000011550 stock solution Substances 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 230000009182 swimming Effects 0.000 description 1
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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
-
- 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
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
Landscapes
- 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)
- Water Treatment By Sorption (AREA)
Abstract
Eliminación de microcontaminantes orgánicos de las aguas mediante el uso de ozono y carbón activado aprovechando la dosis de carbón activado en polvo, comúnmente adicionada en el tratamiento de agua potable, para potenciar la eficacia depurativa del ozono en la eliminación de microcontaminantes orgánicos de gran toxicidad. El sistema consta de un ozonizador, un contactor para favorecer la transferencia del ozono desde la fase gaseosa hasta la fase acuosa, un sensor de ozono en fase acuosa con el fin de valuar de forma continua la concentración de ozono en el reactor, una bomba peristáltica para bombear el agua a través del reactor en columna, un depósito de carbón activado con una válvula para controlar la dosis de carbón adicionada al sistema y, finalmente, un sistema de separación de fases, que permita la completa eliminación del carbón activado en polvo adicionado.Elimination of organic microcontaminants from water through the use of ozone and activated carbon by taking advantage of the dose of activated carbon powder, commonly added in the treatment of drinking water, to enhance the purification efficiency of ozone in the elimination of highly toxic organic microcontaminants. The system consists of an ozonator, a contactor to promote the transfer of ozone from the gas phase to the aqueous phase, an ozone sensor in the aqueous phase in order to continuously assess the concentration of ozone in the reactor, a peristaltic pump to pump the water through the column reactor, an activated carbon tank with a valve to control the dose of carbon added to the system and, finally, a phase separation system, which allows the complete removal of the activated carbon powder added .
Description
Sistema de eliminación de microcontaminantes orgánicos de las aguas mediante el uso de ozono y carbón activado.Microcontaminant removal system organic water through the use of ozone and coal activated.
Sistema de tratamiento basado en el uso simultáneo de ozono y carbón activado en polvo para la eliminación de microcontaminantes orgánicos presentes en aguas.Use based treatment system simultaneous ozone and activated carbon powder for disposal of organic microcontaminants present in waters.
La gran sensibilidad despertada últimamente por la calidad del agua, ha conseguido que se inviertan gran cantidad de recursos humanos y monetarios, tanto por parte de las administraciones públicas como de las agencias privadas, en el desarrollo de nuevos procesos de tratamiento de aguas de gran efectividad en la eliminación de microcontaminantes orgánicos, altamente nocivos para la salud humana.The great sensitivity aroused lately by water quality, has managed to invest a lot of human and monetary resources, both by the public administrations as of private agencies, in the development of new large water treatment processes effectiveness in the elimination of organic microcontaminants, highly harmful to human health.
En el caso de los microcontaminantes orgánicos se ha sugerido el uso del ozono, debido a su elevada capacidad oxidante, como alternativa depurativa para su degradación (von Gunten, U. Ozonation of drinking water: Part I. Oxidation kinetics and product formation. Water Research, 37, 1443-1467, 2003; von Gunten U., Ozonation of drinking water: Part II. Disinfection and by-product formation in presence of bromide, iodide and chlorine, Water Research, 37, 1469-1487, 2003). Sin embargo, este proceso se encuentra limitado por la cinética química, así como por la posible generación de compuestos intermedios de mayor toxicidad que el compuesto de partida. Por ello, con el fin de incrementar la eficacia depurativa del ozono, así como reducir el consumo del mismo para alcanzar un nivel de depuración determinado, surgieron los procesos de oxidación avanzada, O_{3}/H_{2}O_{2}, O_{3}/OH^{-}, O_{3}/UV, (Glaze W.H., Kang J.W., Chapin D.H., The chemistry of water treatment processes involving ozone, hydrogen peroxide and ultraviolet radiation. Ozone Science and Engineering, 9, 335-342, 1987; Bermond A. and Camel V. The use of ozone and associated oxidation processes in drinking water treatment. Water Research, 32, 3208-3222, 1998). Estos procesos se basan en la descomposición del ozono en radicales \cdotOH, los cuales se caracterizan por presentar una alta reactividad y un gran potencial oxidante, atacando a la mayor parte de las moléculas orgánicas, mediante reacciones con constantes de velocidad que oscilan entre 10^{6} y 10^{9} M^{-}^{1}s^{-1}. De todos estos sistemas, el único que es aplicado en los procesos de depuración de aguas destinadas a consumo humano a escala real, debido a su fácil aplicación y bajo coste económico, es el basado en el uso de O_{3}/H_{2}O_{2}.In the case of organic microcontaminants, the use of ozone has been suggested, due to its high oxidizing capacity, as a purifying alternative for its degradation (von Gunten, U. Ozonation of drinking water: Part I. Oxidation kinetics and product formation. Water Research , 37, 1443-1467, 2003 ; von Gunten U., Ozonation of drinking water: Part II. Disinfection and by-product formation in presence of bromide, iodide and chlorine, Water Research , 37, 1469-1487, 2003 ). However, this process is limited by chemical kinetics, as well as by the possible generation of intermediate compounds of greater toxicity than the starting compound. Therefore, in order to increase the purification efficiency of ozone, as well as reduce its consumption to reach a certain level of purification, the advanced oxidation processes, O_ {3} / H_ {2} 2, arose O 3 / OH -, O 3 / UV, (Glaze WH, Kang JW, Chapin DH, The chemistry of water treatment processes involving ozone, hydrogen peroxide and ultraviolet radiation. Ozone Science and Engineering , 9, 335-342, 1987 ; Bermond A. and Camel V. The use of ozone and associated oxidation processes in drinking water treatment. Water Research , 32, 3208-3222, 1998 ). These processes are based on the decomposition of ozone into radicals \ OH, which are characterized by high reactivity and high oxidative potential, attacking most of the organic molecules, through reactions with velocity constants ranging between 10 ^ {6} and 10 <9> M <-1> s <-1>. Of all these systems, the only one that is applied in water purification processes destined for human consumption on a real scale, due to its easy application and low economic cost, is the one based on the use of O_ {3} / H_ {2 } O_ {2}.
Recientemente, se están investigando nuevas alternativas a los procesos de oxidación avanzada tradicionales comentados anteriormente. Estas alternativas se basan en la adición de metales pesados al sistema (Cr_{2}O_{3}r ZnSO_{4}, CuSO_{4}, entre otros) para aumentar la extensión del proceso de ozonización de los microcontaminantes orgánicos (Abdo M.S.E., Shaban H., Bader M.S.H. Decolorization by ozone of direct dyes in presence of some catalysts. J. Environ. As. Health, A23, 697-708, 1988; Andreozzi R. Insola A., Caprio V., D'amore M.G. The kinetics of Mn(ll)-catalysed ozonation of oxalic acid in aqueous solution. Water Research, 26, 917-925, 1992; Sánchez-Polo M. and Rivera-Utrilla J. Metal-catalyzed ozonation of 1,3,6-naphthalenetrisulphonic acid. J. Chem. Tech. Biotech., (Aceptado (en prensa), 2004). Este proceso ha recibido el nombre de "ozonización catalítica homogénea" y el mecanismo implicado así como la influencia de los parámetros operacionales en este proceso, son aún motivo discusión en los diferentes foros científicos. Además, la necesidad de añadir estos metales al medio incrementa la toxicidad del sistema dificultando, de este modo, su posible aplicación práctica.Recently, new alternatives to the traditional advanced oxidation processes discussed above are being investigated. These alternatives are based on the addition of heavy metals to the system (Cr 2 O 3 {r} ZnSO_ {4}, CuSO_ {4}, among others) to increase the extension of the ozonation process of organic microcontaminants (Abdo MSE , Shaban H., Bader MSH Decolorization by ozone of direct dyes in presence of some catalysts. J. Environ. As. Health , A23, 697-708, 1988 ; Andreozzi R. Insola A., Caprio V., D'amore MG The kinetics of Mn (ll) -catalysed ozonation of oxalic acid in aqueous solution.Water Research , 26, 917-925, 1992 ; Sánchez-Polo M. and Rivera-Utrilla J. Metal-catalyzed ozonation of 1,3,6- naphthalenetrisulphonic acid. J. Chem. Tech. Biotech. , (Accepted (in press), 2004 ). This process has been called "homogeneous catalytic ozonation" and the mechanism involved as well as the influence of operational parameters in this process, they are still a reason for discussion in the different scientific forums, and the need to add these metals to the environment increases the toxicity This system makes it difficult, in this way, its possible practical application.
Todas las metodologías anteriormente propuestas, persiguen potenciar la degradación de los microcontaminantes orgánicos acelerando el proceso de descomposición del ozono en radicales \cdotOH. Sin embargo, debido a su alta reactividad, estos radicales presentan una baja selectividad, por lo que pueden ser consumidos en reacciones con compuestos que, normalmente, se encuentran en las fuentes de agua destinadas a consumo humano tales como carbonatos y bicarbonatos, que actúan como atrapadores de radicales \cdotOH, deteniendo las reacciones de propagación involucradas en el proceso de oxidación. Por tanto, la presencia de tales agentes inhibidores de radicales \cdotOH en las aguas puede reducir la efectividad de estos sistemas de tratamiento en la oxidación de los microcontaminantes orgánicos, provocando un incremento en el consumo de ozono para lograr un grado de depuración determinado. Además, una baja eficiencia en la utilización del ozono durante el proceso de oxidación de los microcontaminantes orgánicos puede dar lugar a la formación de compuestos de mayor toxicidad que el compuesto de partida, así como a un mayor coste económico del proceso depurativo.All the previously proposed methodologies, seek to enhance the degradation of microcontaminants organic accelerating the process of ozone decomposition in radicals \ OH. However, due to its high reactivity, these radicals have low selectivity, so they can be consumed in reactions with compounds that normally found in water sources intended for human consumption such as carbonates and bicarbonates, which act as trappers of radicals \ OH, stopping the propagation reactions involved in the oxidation process. Therefore, the presence of such radical inhibitors? in the water can reduce the effectiveness of these treatment systems in the oxidation of organic microcontaminants, causing a increase in ozone consumption to achieve a degree of Debugging determined. In addition, a low efficiency in the use of ozone during the oxidation process of Organic microcontaminants can lead to the formation of compounds of greater toxicity than the starting compound, as well as at a higher economic cost of the purification process.
Con el fin de evitar estos problemas, se ha sugerido el uso de catalizadores sólidos para acelerar la velocidad de ozonización de microcontaminantes de baja biodegradabilidad. La ``ozonización catalítica heterogénea esta muy poco estudiada y es difícil encontrar datos bibliográficos en este área, aparte de algunos escuetos informes técnicos protegidos por el celo industrial de la aplicación de esta novedosa tecnología.In order to avoid these problems, it has suggested the use of solid catalysts to accelerate the speed of ozonation of microcontaminants of low biodegradability. The `` Heterogeneous catalytic ozonation is very poorly studied and is difficult to find bibliographic data in this area, apart from some brief technical reports protected by industrial zeal of the application of this new technology.
La utilización combinada de ozono y carbón
activado granular (GAC), en un mismo proceso de tratamiento, ha
sido identificada en los últimos años como una opción atractiva
para destruir microcontaminantes orgánicos de gran toxicidad. Se ha
demostrado que la combinación del alto poder oxidante del ozono y la
alta capacidad de adsorción del GAC, permite una efectiva
eliminación de los microcontaminantes orgánicos de alta toxicidad y
baja biodegradabilidad (Mackay G. and McAleavey G. Ozonation and
carbon adsorption in a three-phase fluidised bed
for colour removal from peat water. Chem. Eng. Res. Des.,
66, 532-536, 1988; Zaror C.A. Enhanced
oxidation of toxic effluents using simultaneous ozonation and
activated carbon treatment. J. Chem. Tech. and Biotech., 70,
21-28, 1997). Además, estudios recientes
(Rivera-Utrilla et al., Effect of
ozone/activated carbon treatments on genotoxic activity of
naphthalenesulphonic acids. J. of Chem. Tech. and Biotech.,
77, 883-890, 2002;
Rivera-Utrilla J. and Sánchez-Polo
M. Ozonation of 1,3,6-naphthalenetrisulphonic acid
catalyzed by activated carbon in aqueous phase. Appl. Catalysis
B: Environmental, 39, 319-329, 2002;
Sánchez-Polo M. and Rivera-Utrilla
J. Effect of the ozone-carbon reaction on the
catalytic activity of activated carbon during the degradation of
1,3,6-naphthalenesulphonic acid with ozone.
Carbon, 41, 303-307, 2003) han
demostrado que el GAC actúa también, como iniciador/promotor del
proceso de transformación del ozono en radicales \cdotOH
incrementando, de este modo, la eficacia depurativa de este sistema,
ya que estas especies son altamente reactivas, atacando a los
compuestos orgánicos rápidamente y provocando, en algunas
ocasiones, la transformación de la materia orgánica disuelta en
dióxido de carbono.The combined use of ozone and granular activated carbon (GAC), in the same treatment process, has been identified in recent years as an attractive option to destroy highly toxic organic microcontaminants. It has been shown that the combination of the high oxidant power of ozone and the high adsorption capacity of GAC, allows an effective elimination of organic microcontaminants of high toxicity and low biodegradability (Mackay G. and McAleavey G. Ozonation and carbon adsorption in a three -phase fluidised bed for color removal from peat water. Chem. Eng. Res. Des. , 66, 532-536, 1988 ; Zaror CA Enhanced oxidation of toxic effluents using simultaneous ozonation and activated carbon treatment. J. Chem. Tech. and Biotech. , 70, 21-28, 1997 ). In addition, recent studies (Rivera-Utrilla et al ., Effect of ozone / activated carbon treatments on genotoxic activity of
Naphthalenesulphonic acids. J. of Chem. Tech. And Biotech. , 77, 883-890, 2002 ; Rivera-Utrilla J. and Sánchez-Polo M. Ozonation of 1,3,6-naphthalenetrisulphonic acid catalyzed by activated carbon in aqueous phase. Appl. Catalysis B: Environmental , 39, 319-329, 2002 ; Sánchez-Polo M. and Rivera-Utrilla J. Effect of the ozone-carbon reaction on the catalytic activity of activated carbon during the degradation of 1,3,6-naphthalenesulphonic acid with ozone. Carbon , 41, 303-307, 2003 ) have shown that GAC also acts as an initiator / promoter of the process of transforming ozone into radicals \ cdotOH, thereby increasing the purification efficiency of this system, since these species are highly reactive, attacking organic compounds rapidly and sometimes causing the transformation of dissolved organic matter into carbon dioxide.
Desde el descubrimiento de la actividad catalítica del carbón activado granular (GAC) en el proceso transformación del ozono en radicales \cdotOH (Rivera-Utrilla J. and Sánchez-Polo M. Ozonation of 1,3,6-naphthalenetrisulphonic acid catalyed by activated carbon in aqueous phase. Appl. Catalysis B: Environmental, 39, 319-329, 2002; Sánchez-Polo M. and Rivera-Utrilla J. Effect of the ozone-carbon reaction on the catalytic activity of activated carbon during the degradation of 1,3,6-naphthalenesulphonic acid with ozone. Carbon, 41, 303-307, 2003), numerosos están siendo numerosos los esfuerzos destinados a mejorar la eficacia depurativa de este sistema (O_{3}/GAC) con el fin de acelerar su implementación a escala real (Beltrán F.J., Rivas J., Alvarez P., Montero de Espinosa R., Kinetics of heterogeneous catalytic ozone decomposition in water in an activated carbon. Ozone Science and Engineering, 24, 227-237, 2002; Ma J., Sui M.H., Chen Z.L., Wang L.N., Degradation of refractory organic pollutants by catalytic ozonation. Activated carbon and Mn-loaded activated carbon as catalyst. Ozone Science and Engineering, 26, 3-10, 2004).Since the discovery of the catalytic activity of granular activated carbon (GAC) in the process of transforming ozone into radicals \ cdotOH (Rivera-Utrilla J. and Sánchez-Polo M. Ozonation of 1,3,6-naphthalenetrisulphonic acid catalyzed by activated carbon in aqueous phase. Appl. Catalysis B: Environmental , 39, 319-329, 2002 ; Sánchez-Polo M. and Rivera-Utrilla J. Effect of the ozone-carbon reaction on the catalytic activity of activated carbon during the degradation of 1, 3,6-naphthalenesulphonic acid with ozone Carbon , 41, 303-307, 2003 ), numerous efforts are being made to improve the purification efficiency of this system (O3 / GAC) in order to accelerate its implementation full scale (Beltrán FJ, Rivas J., Alvarez P., Montero de Espinosa R., Kinetics of heterogeneous catalytic ozone decomposition in water in an activated carbon. Ozone Science and Engineering , 24, 227-237, 2002 ; Ma J. , Sui MH, Chen ZL, Wang LN, Degradation of refractory orga nic pollutants by catalytic ozonation. Activated carbon and Mn-loaded activated carbon as catalyst. Ozone Science and Engineering , 26, 3-10, 2004).
El nuevo sistema de tratamiento propuesto está destinado principalmente a la depuración de aguas destinadas a consumo humano y efluentes industriales. En el caso de los efluentes industriales, el sistema basado en el uso simultáneo de ozono y carbón activado en polvo se podría usar como etapa previa al tratamiento biológico secundario, potenciando así la trasformación de los microcontaminantes de elevada toxicidad en compuestos orgánicos de gran biodegradabilidad y facilitando, de este modo, la acción depurativa de los microorganismos. Igualmente, en otras ocasiones, dependiendo de las características químicas del efluente industrial, el sistema depurativo planteado también se podría usar, con el mismo fin, al final del proceso depurativo (tratamiento terciario). El nuevo sistema de tratamiento propuesto reduce considerablemente el olor, color y demanda química de oxígeno del efluente tratado.The proposed new treatment system is intended primarily for the purification of water intended for human consumption and industrial effluents. In the case of industrial effluents, the system based on the simultaneous use of ozone and activated carbon powder could be used as a pre-stage secondary biological treatment, thus enhancing the transformation of microcontaminants of high toxicity in compounds organic biodegradability and thus facilitating the depurative action of microorganisms. Likewise, in others occasions, depending on the chemical characteristics of the effluent industrial, the proposed purification system could also be used, for the same purpose, at the end of the purification process (treatment tertiary). The proposed new treatment system reduces considerably the smell, color and chemical oxygen demand of the treated effluent.
En el tratamiento de aguas destinadas a consumo humano, el sistema basado en el uso simultáneo de ozono y carbón activado en polvo se podría usar como tratamiento previo, con el fin de eliminar Fe, Mn, y microcontaminantes orgánicos. Además, con este tratamiento se facilita el proceso posterior de coagulación/sedimentación. De forma similar, el sistema propuesto se puede usar en una etapa intermedia para eliminar la materia orgánica natural del agua y potenciar la transformación de microcontaminantes orgánicos en compuestos de mayor biodegradabilidad reduciendo, de esta forma, las propiedades organolépticas del agua. Este hecho también incrementa la eficiencia de los filtros de carbón activado y evita la formación de compuestos organoclorados de gran toxicidad durante la etapa final de cloración.In the treatment of water intended for consumption human, the system based on the simultaneous use of ozone and coal Powdered activated could be used as a pretreatment, with the in order to eliminate Fe, Mn, and organic microcontaminants. Also with This treatment facilitates the subsequent process of coagulation / sedimentation. Similarly, the proposed system will be can use at an intermediate stage to remove matter Natural organic water and enhance the transformation of organic microcontaminants in higher compounds biodegradability reducing, in this way, the properties Water organoleptic. This fact also increases efficiency of activated carbon filters and prevents the formation of Highly toxic organochlorine compounds during the final stage Chlorination
Otra de las posibles aplicaciones de este novedoso sistema de tratamiento es en la depuración de aguas de las piscinas. La recirculación de estas aguas a través de un reactor adecuado para ello reduciría el consumo de ozono necesario para alcanzar el nivel de depuración exigido en las mismas.Another of the possible applications of this Novel treatment system is in the purification of water from the swimming pools. The recirculation of these waters through a reactor suitable for this would reduce the ozone consumption needed to reach the level of purification required in them.
El sistema de tratamiento basado en el uso simultáneo de ozono y carbón activado en polvo (PAC) surge con el fin de disminuir la dosis de ozono necesaria para eliminar los microcontaminantes orgánicos presentes en las aguas destinadas a consumo humano reduciendo, de esta forma, el coste económico del tratamiento depurativo. El sistema de tratamiento propuesto aprovecha la dosis de carbón activado en polvo adicionada en la depuración de aguas destinadas a consumo humano, para incrementar la eficacia depurativa del ozono. Ambos sistemas, ozono y carbón activado en polvo, son sistemas de tratamiento utilizados, comúnmente por separado, en la depuración de aguas destinadas a consumo humano por lo que, el nuevo sistema depurativo propuesto, basado en el uso simultáneo de ozono y carbón activado en polvo (O_{3}/PAC), es de muy fácil aplicación y bajo coste de implementación.The use-based treatment system Simultaneous ozone and activated carbon powder (PAC) arises with the in order to reduce the dose of ozone necessary to eliminate organic microcontaminants present in waters intended for human consumption thus reducing the economic cost of depurative treatment The proposed treatment system take advantage of the dose of activated carbon powder added in the purification of water intended for human consumption, to increase the purification efficiency of ozone. Both systems, ozone and coal Powdered activated, are treatment systems used, commonly separately, in the purification of water intended for human consumption so, the proposed new purification system, based on the simultaneous use of ozone and activated carbon powder (O_ {3} / PAC), it is very easy to apply and low cost implementation.
Se ha observado que al usar carbón activado granular (GAC) con un tamaño de partícula superior a 200-500 \mum la velocidad de transformación del ozono en radicales \cdotOH depende, notablemente, del proceso de difusión intraparticular del mismo en la superficie del carbón activado reduciéndose, de esta forma, la eficacia de este material en el proceso de transformación del ozono en radicales \cdotOH. Por ello, en la presente invención, con el fin de eliminar el efecto de los fenómenos difusionales en el sistema O_{3}/GAC y potenciar de esta forma el proceso de transformación del ozono en radicales \cdotOH, se utiliza carbón activado en polvo (PAC) como agente catalizador del proceso de ozonización de microcontaminantes orgánicos.It has been observed that when using activated carbon granular (GAC) with a particle size greater than 200-500 µm the transformation speed of the ozone in radicals \ cdotOH depends, notably, on the process of intraparticular diffusion of it on the surface of the coal activated thereby reducing the effectiveness of this material in the process of transforming ozone into radicals \ cdOTOH. Therefore, in the present invention, in order to eliminate the effect of diffusional phenomena in the O3 / GAC system and enhance in this way the process of transforming ozone into radicals • Powdered activated carbon (PAC) is used as agent catalyst for the ozonation process of microcontaminants organic
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El sistema de tratamiento propuesto aprovecha la dosis de PAC, usualmente adicionada en el tratamiento de agua potable (1 - 100 mg/L), para potenciar la eficacia depurativa del ozono en la eliminación de microcontaminantes orgánicos de gran toxicidad. El sistema consiste en adicionar bajas concentraciones de carbón activado en polvo durante el proceso de ozonización de las aguas. Posteriormente, el carbón activado adicionado será eliminado de las aguas tratadas mediante el uso de alguno de los diferentes sistemas de separación de fases existentes en la actualidad (floculación/precipitación, centrifugación, separación por membranas...).The proposed treatment system takes advantage of the dose of CAP, usually added in water treatment drinkable (1 - 100 mg / L), to enhance the purifying efficacy of ozone in the elimination of large organic microcontaminants toxicity. The system consists of adding low concentrations of activated carbon powder during the ozonation process of waters Subsequently, the added activated carbon will be removed of treated waters by using any of the different phase separation systems currently in existence (flocculation / precipitation, centrifugation, separation by membranes ...).
El nuevo sistema de tratamiento de aguas constaría, por tanto, de un ozonizador, un contactor para favorecer la transferencia del ozono desde la fase gaseosa hasta la fase acuosa, un sensor de ozono en fase acuosa con el fin de valuar de forma continua la concentración de ozono en el reactor, una bomba peristáltica para bombear el agua a través del reactor en columna, un depósito de carbón activado con una válvula para controlar la dosis de carbón adicionada al sistema y, finalmente, un sistema de separación de fases, que permita la completa eliminación del carbón activado en polvo adicionado.The new water treatment system It would consist, therefore, of an ozonator, a contactor to favor the transfer of ozone from the gas phase to the phase aqueous, an aqueous phase ozone sensor in order to value continuously form the concentration of ozone in the reactor, a pump peristaltic to pump water through the column reactor, an activated carbon tank with a valve to control the dose of carbon added to the system and finally a system of phase separation, which allows complete carbon removal Powdered activated added.
El sistema de tratamiento propuesto (O_{3}/PAC) se ha utilizado para la eliminación de microcontaminantes orgánicos, usando como compuesto modelo, el dodecilbencensulfonato de sodio (SDBS). Este es un surfactante de amplia aplicación, tanto en el sector doméstico como en el sector industrial. La utilización de tratamientos convencionales (tratamiento biológico, ozono) en la eliminación de este contaminante ha resultado no ser muy efectiva provocando, en algunas ocasiones, la generación de subproductos de oxidación más tóxicos que el producto de partida.The proposed treatment system (O_ {3} / PAC) has been used for the removal of organic microcontaminants, using as a model compound, the sodium dodecylbenzenesulfonate (SDBS). This is a surfactant of wide application, both in the domestic sector and in the sector industrial. The use of conventional treatments (biological treatment, ozone) in the elimination of this pollutant has turned out not to be very effective causing some occasions, the generation of oxidation byproducts more Toxic than the starting product.
El sistema experimental usado para llevar a cabo este estudio, consistió en un generador de ozono cuya capacidad máxima es de 76 mg O_{3}/min, un reactor con agitación de 1 litro (260 r.p.m.), y un espectrofotómetro como se muestra en la Figura 1, donde se indican los detalles de este sistema.The experimental system used to carry out This study consisted of an ozone generator whose capacity maximum is 76 mg O3 / min, a 1 liter stirred reactor (260 r.p.m.), and a spectrophotometer as shown in Figure 1, where the details of this system are indicated.
Para llevar a cabo estas experiencias, el reactor se llena con un 1 L de disolución reguladora del pH deseado. La corriente mezcla ozono-oxígeno es dirigida hacia el espectrofotómetro donde se analiza la presión parcial de ozono antes de introducirla en el reactor. Una vez ajustadas la presión parcial de ozono y la temperatura deseada en el reactor, la corriente gaseosa se introduce en el mismo, durante un periodo determinado, hasta conseguir la concentración de ozono deseada. Posteriormente, y sin dejar de suministrar ozono al reactor, se adiciona una alícuota de la disolución stock de SDBS y la dosis adecuada de PAC (2.5-100 mg/L). A intervalos regulares de tiempo son retiradas varias muestras del reactor para evaluar la concentración de SDBS, la concentración de ozono disuelto y el carbono orgánico disuelto (DOC) en función del tiempo del tratamiento. El ozono residual fue eliminado mediante el uso de nitrito sódico.To carry out these experiences, the reactor is filled with a 1 L of pH regulating solution wanted. The ozone-oxygen mixture stream is directed towards the spectrophotometer where the pressure is analyzed partial ozone before introducing it into the reactor. One time adjusted the partial pressure of ozone and the desired temperature in the reactor, the gas stream is introduced therein, during a certain period, until the ozone concentration is achieved desired. Subsequently, and while still providing ozone to the reactor, an aliquot of the stock solution of SDBS is added and the appropriate dose of CAP (2.5-100 mg / L). TO regular intervals of time several samples of the reactor to evaluate the concentration of SDBS, the concentration of dissolved ozone and dissolved organic carbon (DOC) depending on the treatment time The residual ozone was removed by use of sodium nitrite.
Los resultados obtenidos al llevar a cabo la ozonización del SDBS en ausencia y presencia del carbón activado (Sorbo) granular (GAC) y en polvo (PAC), así como las cinéticas de adsorción del SDBS sobre los distintos carbones activados estudiados se presentan en la Figura 2. En esta Figura se puede observar la baja reactividad del SDBS frente al ozono, y como la presencia de carbón activado, especialmente PAC, durante el proceso de ozonización del SDBS acelera notablemente la velocidad de eliminación del mismo del medio.The results obtained when carrying out the ozonation of the SDBS in the absence and presence of activated carbon (Sorbo) granular (GAC) and powder (PAC), as well as the kinetics of adsorption of SDBS on the different activated carbons studied are presented in Figure 2. In this Figure you can observe the low reactivity of the SDBS against ozone, and how the presence of activated carbon, especially PAC, during the process ozonation of the SDBS significantly accelerates the speed of elimination of it from the medium.
La mayor velocidad de adsorción de contaminantes orgánicos por parte del PAC frente al GAC es ampliamente conocida y se debe principalmente a una reducción de los fenómenos difusionales del SDBS en la superficie del carbón activado y a una mayor homogenización del sistema, que favorece el contacto entre el SDBS y la superficie del carbón activado. De acuerdo con los resultados presentados en la Figura 2, el incremento en la velocidad de eliminación del SDBS debido a la presencia de GAC durante el proceso de ozonización del mismo es debido, exclusivamente, a la generación de radicales \cdotOH en la interacción O_{3}/carbón activado (contribución catalítica) mientras que, por el contrario existe una gran contribución del proceso adsortivo al proceso global de eliminación del SDBS al adicionar PAC al sistema. De esta forma, con los resultados presentados en la Figura 2, es posible determinar que para el sistema basado en el uso conjunto de O_{3}/PAC, se puede deducir que después de 10 min de tratamiento (tiempo usual de retención hidráulico) la contribución adsortiva al proceso global de eliminación del SDBS es de un 60% mientras que la contribución catalítica, debida a la generación de radicales \cdotOH en el sistema, es de un 40%, muy superior a la determinada en el sistema basado en el uso de O_{3}/GAC (20%). Estos resultados fueron corroborados al llevar a cabo la determinación de la constante de descomposición del ozono mediante un modelo cinético de primer orden (k_{D}). Así, el valor de k_{D} observado para el sistema O_{3}/PAC (k_{D} = 8.4 10^{-3} s^{-1}) fue 3.5 veces superior al valor observado para el sistema O_{3}/GAC (k_{D} = 2.3 10^{-3} s^{-1}). Por tanto, los valores de k_{D} obtenidos indican que la presencia de PAC durante el proceso de ozonización del SDBS acelera en mayor medida la velocidad de generación de radicales \cdotOH en el sistema incrementando, de esta forma, la velocidad de eliminación del SDBS del medio.The highest adsorption rate of contaminants organic by the PAC versus the GAC is widely known and It is mainly due to a reduction in phenomena diffusional SDBS on the surface of activated carbon and at a greater homogenization of the system, which favors contact between the SDBS and the surface of activated carbon. I agree with you results presented in Figure 2, the increase in SDBS removal rate due to the presence of GAC during the ozonation process it is due, exclusively, to the generation of radicals \ cdotOH in the O 3 / activated carbon interaction (catalytic contribution) whereas, on the contrary there is a great contribution of adsorptive process to the global SDBS elimination process by add CAP to the system. In this way, with the results presented in Figure 2, it is possible to determine that for system based on the joint use of O_ {3} / PAC, can be deduced that after 10 min of treatment (usual retention time hydraulic) the adsorptive contribution to the overall process of SDBS removal is 60% while the contribution catalytic, due to the generation of radicals? in the system, is 40%, much higher than that determined in the system based on the use of O 3 / GAC (20%). These results were corroborated when carrying out the determination of the constant of ozone decomposition through a first kinetic model order (k_ {D}). Thus, the value of k_ {D} observed for the system O 3 / PAC (k D = 8.4 10 -3 s -1) was 3.5 times greater than the value observed for the O_ {3} / GAC system (k_ {D} = 2.3 10 -3 s -1). Therefore, the values of k_ {D} obtained indicate that the presence of CAP during the ozonation process SDBS accelerates the generation speed of radicals \ cdotOH in the system thereby increasing the SDBS removal rate from the medium.
Debido a la baja selectividad de los radicales \cdotOH, un parámetro muy importante que afecta considerablemente la eficacia de los sistemas de oxidación avanzada en la eliminación de microcontaminantes orgánicos es la presencia de atrapadores de radicales en el sistema. Así, en las aguas destinadas a consumo humano el principal agente atrapador de radicales es el anión HCO_{3}^{-} (k_{OH} = 8.5 10^{6} M^{-1}s^{-1}). Los resultados obtenidos han mostrado que la presencia de bajas concentraciones HCO_{3}^{-} en el medio no reduce, considerablemente, la eficacia depurativa del sistema basado en el uso de O_{3}/PAC, como ocurre con el resto de procesos de oxidación comúnmente utilizados en el tratamiento de aguas destinadas a consumo humano (O_{3}, O_{3}/H_{2}O_{2}).Due to the low selectivity of the radicals \ cdotOH, a very important parameter that affects considerably The effectiveness of advanced oxidation systems in elimination of organic microcontaminants is the presence of trappers of radicals in the system. Thus, in the waters destined for consumption human the main radical trapping agent is anion HCO 3 - (k OH = 8.5 10 6 M -1 s -1). The results obtained have shown that the presence of casualties HCO 3 - concentrations in the medium does not reduce, considerably, the purifying efficiency of the system based on the use of O_ {3} / PAC, as with the rest of the processes of oxidation commonly used in water treatment intended for human consumption (O 3, O 3 / H 2 O 2).
Un parámetro muy importante para evaluar la eficacia depurativa de un sistema de tratamiento es su capacidad para retirar materia orgánica disuelta (TOC). En la Figura 3 se observa la evolución de la concentración de TOC en función del tiempo de tratamiento para cada uno de los sistemas estudiados (O_{3}, PAC y O_{3}/PAC). Los resultados obtenidos indican que el sistema basado en el uso exclusivo de O_{3} no reduce la concentración de materia orgánica disuelta, indicando que este sistema no tiene el potencial oxidante suficiente para provocar la transformación de la misma en CO_{2}. Sin embargo, en el caso del sistema basado en el uso conjunto de O_{3}/PAC se puede observar que a los 30 min de tratamiento la concentración de TOC se ve reducida en un 80%.A very important parameter to evaluate the Purifying effectiveness of a treatment system is its ability to remove dissolved organic matter (TOC). Figure 3 shows observe the evolution of the TOC concentration as a function of treatment time for each of the systems studied (O 3, PAC and O 3 / PAC). The results obtained indicate that the system based on the exclusive use of O_ {3} does not reduce the concentration of dissolved organic matter, indicating that this system does not have enough oxidant potential to cause the transformation of it into CO2. However, in the case of system based on the joint use of O_ {3} / PAC can be observed that after 30 min of treatment the TOC concentration is seen reduced by 80%.
Así, los resultados obtenidos indican que además del papel iniciador/promotor desempeñado por el carbón activado en el proceso de ozonización, favoreciendo la transformación del ozono disuelto en radicales \cdotOH y, por tanto, potenciando la degradación de microcontaminantes orgánicos resistentes al ozono, éste también presenta un papel adsorbente, retirando materia orgánica de las aguas incrementando, de esta forma, la eficacia depurativa del sistema.Thus, the results obtained indicate that in addition of the initiator / promoter role played by activated carbon in the ozonation process, favoring the transformation of ozone dissolved in radicals \ OH and, therefore, enhancing the degradation of ozone resistant organic microcontaminants, It also has an adsorbent role, removing matter organic water, thus increasing the efficiency system purification.
Figura 1. Sistema experimental utilizado. 1, Oxígeno; 2, Ozonizador; 3, Reactor; 4, Espectrofotómetro; 5, Medidor de Flujo; 6, Trampa de carbón activado.Figure 1. Experimental system used. one, Oxygen; 2, Ozonator; 3, Reactor; 4, Spectrophotometer; 5, Flowmeter; 6, Activated carbon trap.
Figura 2. Eliminación del SDBS mediante los distintos sistemas estudiados. pH 7, [SDBS]_{0} = 2.8 10^{-5} M, T 298 K, [O_{3}] = 2 10^{-5} M, [Carbón activado] = 100 mg/L.Figure 2. Elimination of SDBS by means of Different systems studied. pH 7, [SDBS] 0 = 2.8 10-5 M, T 298 K, [O3] = 2 10-5 M, [Activated Carbon] = 100 mg / L
(x), O_{3}; (\medcirc), O_{3}/GAC; (\boxempty), O_{3}/PAC; (\ding{115}), PAC; (\medbullet), GAC. En el eje de abcisas se representa el tiempo, t, en minutos, mientras que en el eje de ordenadas se representa la relación, R, entre la concentración de SDBS observada para cada tiempo y la concentración inicial de SDBS presente en el sistema ([SDBS]t/[SDBS]_{0}). O indica Ozonización y A indica Adsorción.(x), O 3; (med), O 3 / GAC; (\ boxempty), O_ {3} / PAC; ({{115}), PAC; (?), GAC. In the axis of abscissa the time, t , in minutes is represented, while in the axis of ordinates the relation, R , between the concentration of SDBS observed for each time and the initial concentration of SDBS present in the system ([ SDBS] t / [SDBS] 0). O indicates Ozonation and A indicates Adsorption.
Figura 3. Evolución de la concentración de TOC en función del tiempo de tratamiento para los distintos sistemas estudiados. pH 7, [SDBS]_{0} = 2.8 10^{-5} M, T 298 K, [O_{3}] = 2 10^{-5} M, [PAC] = 100 mg/L. (x), O_{3}; (\ding{115}), PAC; (\boxempty), O_{3}/PAC. En el eje de abcisas se representa el tiempo, t, en minutos, mientras que en el eje de ordenadas se representa la relación, R, entre la concentración de TOC observada para cada tiempo y la concentración inicial de TOC presente en el sistema ([TOC]_{t}/[TOC]_{0}).Figure 3. Evolution of the TOC concentration as a function of the treatment time for the different systems studied. pH 7, [SDBS] 0 = 2.8 10-5 M, T 298 K, [O 3] = 2 10-5 M, [PAC] = 100 mg / L. (x), O 3; ({{115}), PAC; (\ boxempty), O_ {3} / PAC. In the axis of abscissa the time, t , in minutes is represented, while in the axis of ordinates the relation, R , between the concentration of TOC observed for each time and the initial concentration of TOC present in the system ([ TOC] t / [TOC] 0).
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