MX2008010435A

MX2008010435A - Water decontamination systems.

Info

Publication number: MX2008010435A
Application number: MX2008010435A
Authority: MX
Inventors: Davis S Drewelow
Original assignee: Liquid Separation Technologies
Priority date: 2006-02-15
Filing date: 2007-02-14
Publication date: 2009-03-05
Also published as: TW200736177A; BRPI0707840A2; WO2008118111A2; AU2007346964A1; EP1999073A2; CA2678252A1; WO2008118111A3

Abstract

Water decontamination systems including one or more of an aerator module, a separator tower, and a contamination gas treatment system are described herein. Such systems are capable of removing contaminants, including volatile organic compounds, from the water. Certain volatile organic contaminants can be removed at high efficiencies. The systems may be automated to remove the contaminants and produce cleaned water on a continuous basis.

Description

WATER DECONTAMINATION SYSTEMS FIELD OF THE INVENTION The invention is concerned with systems and methods for reducing contaminants in contaminated liquids such as contaminated groundwater.

BACKGROUND OF THE INVENTION Most common sources of water pollution include but are not limited to the environment, the marine and petroleum industries. Water is commonly contaminated with hydrocarbons from fuels such as gasoline, diesel and aviation fuel. The sources of contamination are facilities such as transfer stations, fuel solution terminals, underground storage tanks, military bases, airports, sorting stations, shipyards, dry cleaning plants, plating or metal coating workshops and facilities. manufacture. These facilities regularly contaminate the water with volatile organic compounds (VOC); that is, benzene, toluene, ethylbenzene, xylene (these four compounds are commonly referred to as BTEX); methyl tertiary butyl ether (MTBE), tert-butanol (TBA), trichloroethene (TCE), perchloroethene (PCE) and 1,4-dioxane. Therefore, it is desirable to remove such contaminants from groundwater to comply with regulatory standards.

BRIEF DESCRIPTION OF THE INVENTION [0002] Methods of systems and methods for the purification of contaminated liquids are described herein. According to one embodiment, a system comprises an aerator module, a filter module, a separator tower and a contaminated gas treatment system. However, one or more of these components may be used alone or in conjunction with one or more other components in the purification of liquids. In a preferred embodiment, a liquid decontamination system comprises an aeration module, a separator tower module and a system for treating a contaminated gas. Each of these components is described further herein. Each of the components can be configured to operate under minor operations, equal to or greater than the atmospheric pressure at which the liquid decontamination system is in operation. In the above mode, the aerator module is configured to receive the contaminated liquid. Contaminated liquid can be received from one or more contaminated sources. In a preferred embodiment, the aerator module comprises a tank for receiving the contaminated liquid. In one embodiment, the aerator module comprises a plurality of nozzles that feed a contaminated liquid gas. As the gas is administered to the contaminated liquid, bubbles that They contain the gas formed in the liquid and rise to the tank surface of the aerator module. As the bubbles pass through the contaminated liquid, pollutants from the contaminated liquid change phase from the dissolved pollutant to gaseous pollutants. Gaseous pollutants rise with bubbles in the upper part of the aeration tank. In some embodiments, the aerator module comprises a tank, an air definition manifold and a compressor capable of feeding a gas or a mixture of gases such as compressed air to the air replacement manifold. In some embodiments, the tank is capable of receiving a contaminated liquid through an affluent liquid connection. At least part of the clean air distribution manifold may be contained within the tank comprising the contaminated liquid. In some embodiments, the compressor feeds air or other gas, such as ozone to the air distribution manifold. The manifold of air distribution may comprise one or more orifices that are contained in the tank through which the air is released as bubbles to the contaminated liquid contained in the tank. In some embodiments, the tank comprises deflectors that create a more tortuous path for contaminated bubbles to reach the top of the tank. The tank can be maintained under a partial static vacuum to prevent leakage of contaminants gaseous to the environment. As the bubbles travel through the contaminated liquid, at least some of the pollutants in the contaminated liquid are transferred from the liquid to the gas phase and are removed from the liquid as the bubble leaves the contaminated liquid. This results in a contaminated gas phase in a part of the tank. The contaminated gas phase can be removed by vacuum pump. In some embodiments, the aeration module operates under reduced pressure. One or more vacuum pumps can be adapted to reduce the pressure of the aeration module. As contaminants and bubbles reach the surface of the contaminated liquid, this contaminated liquid can be transported to one or more systems to treat gaseous pollutants by the vacuum pump. Additionally, the residence time for the bubbles in the aeration module can be increased to increase the amount of contaminants fed to the gas phase in the aeration module. For example, the aeration tank may comprise deflectors that create a more tortuous path and an increased resilience time for the bubbles. In a preferred embodiment, the aeration module can operate in a continuous mode. Initially, the aeration tank receives the contaminated liquid. As the aeration tank receives the contaminated liquid, the tank fills up with the contaminated liquid at a fixed level. The fixed level can be designated by a switch or detector. The switch or detector can operate a pump that is capable of transporting the contaminated liquid out of the aeration tank and to one or more components as described herein. As the contaminated liquid is passed out of the aeration tank, the additional contaminated liquid can begin to fill the aeration tank. This process allows the aeration tank to be put into operation continuously. The velocities of the polluted effluent liquid and effluent can be varied to adjust the flow velocities of the contaminated gas and / or efficiency of the aeration module to put contaminants. In some embodiments, contaminated liquid effluent from the aeration tank may be passed to one or more other modules. Such modules include one or more other aeration modules, one or more filter modules, one or more separator tower modules or preferably a separation from any of the foregoing. In a preferred embodiment, the contaminated liquid can be passed to a tower module of the separator. In one embodiment, the separator tower comprises one or more atomization nozzles and a tank configured to receive a liquid with produced levels of contaminants. In one embodiment, the atomization nozzles are capable of receiving the liquid polluted and turn the contaminated liquid into a mist of contaminated liquid. The tank can be put into operation under vacuum. Such reduced pressures can cause the liquid mist to turn into a contaminated gas phase and a liquid phase. In preferred embodiments, the contaminated gas phase is transported out of the separator tower to a system for treating contaminated gases. In one embodiment, the liquid phase comprises a liquid with substantially less contaminants than the contaminated liquid before entering the separating tower module. In one embodiment, the separator tower module can be heated. In another embodiment, the separating tower comprises packing material to increase the residence time of the liquid mist. In another mode, the separating tower can receive dilution air that passes over the liquid mist to remove other contaminants from the liquid fog or atomized contaminated water. In some embodiments, the liquid decontamination system comprises a separating tower. The separator tower may comprise one or more gratings to convert the contaminated liquid to a contaminated gas and an atomized liquid mist phase. The nozzles can be altered to determine the size and atomization of the atomized contaminated liquid. In certain preferred embodiments, the separating tower further comprises a vacuum chamber in which the contaminated liquid is converted to a contaminated gas phase and a liquid fog phase. In some embodiments, the pressure in the vacuum chamber is approximately 50.1 cm Hg (20 inches Hg) to approximately 76 cm Hg (30 inches Hg). In some embodiments, the pressure inside the vacuum chamber is about 56 cm Hg (22 inches Hg) to about 69 cm Hg (27 inches Hg). In some modalities, the pressure is approximately 69 cm Hg (27 inches Hg). The separating tower may additionally comprise a station, wherein the liquid mist may be stored, collected or recycled to the system. In some embodiments, the purified liquid is pumped out of the separating tower while the separating tower maintains its vacuum environment. Additionally, the separator tower may include random packing material upon which the liquid mist is collected in liquid droplets. These drops can then fall to the carcass and be collected. In some embodiments, carrier air (dilution) can be used to assist in the transformation of the contaminated gas phase away from the separating tower. A carrier air may also pass over or through the packing and / or liquid drops and / or liquid mist phase and remove other contaminants from liquid drops and / or liquid mist.

The liquid phase can be collected as purified liquid in the separation tower tank. Such a liquid can then be continuously pumped out of the separating tower. In some embodiments, the liquid comprising less contaminants than the contaminated liquid (the purified liquid) can fill the separating tower. A switch or detector can recognize that the purified liquid has reached a fixed level and put into operation to pump the purified liquid out of the separator tower. In some embodiments, the liquid may be transported to one or more other purification modules, which include but are not limited to one or more aeration tanks, one or more filters and one or more other separator towers. In some embodiments, the purified liquid may be subjected to treatment for animal consumption. The contaminated gas phase can be transported to one or more systems for the treatment of a contaminated gas. Such systems are preferably capable of removing contaminants from the contaminated gas phase. Preferred systems for removing contaminants from the contaminated gas phase may include one or more electrical catalytic oxidants, thermal oxidizers, adsorption filtration systems which include filtration systems by carbon adsorption, zeolite and polymer, condensers, oxidants to the flame, cryogenic treatment processes, processes of gas cooling and liquefaction, regenerative thermal oxidants and rotating concentrators. Methods for decontaminating liquids are also described herein. One modality may include aerating the contaminated liquid, filtering the contaminated liquid, separating the liquid from its remaining contaminants to a contaminated gas phase and a liquid phase in a separating tower under vacuum. Additional modalities may include treatment of the gas phase contaminated with a system for the treatment of contaminated gases. Such a system is capable of reducing the levels of contaminants in the contaminated gas to a safe level, where the gas can be released into the environment. In some embodiments, the treatment may include oxidizing the contaminants. In another embodiment, the treatment may include absorbing the contaminants. In another embodiment, the treatment may include condensation of the contaminants. Simultaneous with or after treatment of the contaminants, the remaining substantially unpolluted gaseous phase is released into the atmosphere. Another embodiment of a method comprises aerating the contaminated liquid under vacuum to remove at least some contaminants from the contaminated liquid and purifying the contaminated gas phase released by the system aerator to treat the contaminated gas. According to some modalities, this can be done in conjunction with the separation of a contaminated liquid to a contaminated gas phase and a liquid fog phase in the separating tower. Both phases of contaminated gas can be processed in the treatment system according to some modalities. One modality of a method to reduce the levels of contaminants in a contaminated liquid involves aerating the contaminated liquid to produce a first phase of contaminated gas, converting the contaminated liquid to a contaminated mist in a separating tower, converting the contaminated mist to a second phase of contaminated gas and a liquid mist by subjecting the contaminated mist to a high vacuum environment within the separation tower and treatment of the first and second phases of contaminated gas in a treatment system. In some embodiments, the above-mentioned treatment step comprises recovering contaminants from the first and second phases of contaminated gas. In some embodiments, the treatment step comprises oxidizing or reducing contaminants from the first and second phases of contaminated gas. In some embodiments, this method further comprises transporting the second phase of contaminated gas out of the separator tower by vacuum. In some embodiments, this method comprises transporting the second phase of contaminated gas away from the separation tower using dilution air. In some modalities, this The method includes combining the first and second phases of contaminated gas before treatment by the treatment system. In some embodiments, the method also includes regulating one or more stages with a controller. As discussed herein, the method can be controlled manually or automatically. In some embodiments of the method mentioned above, clean water is collected from the separating tower. In another embodiment, a method to reduce levels of contaminants in a contaminated liquid includes converting the contaminated liquid to a contaminated mist in a separating tower, converting the contaminated mist to a contaminated gas and a liquid mist by subjecting the contaminated mist to a medium high vacuum environment inside the separator tower and reduce the different pollutants in the gas contaminated by a contaminated gas phase treatment system. In certain embodiments, the contaminated gas treatment system comprises an electrical catalytic oxidant. In certain embodiments, the step of converting the contaminated liquid to a contaminated mist comprises providing the contaminated liquid to an air separator, reducing the pressure of the air separator by a vacuum source, atomizing the contaminated liquid to a contaminated mist through a plurality of nozzles, about the upper part of the air separator, allow the mist to fall gravitationally within the air separator and flow the air in a direction countercurrent to the fall by gravitation of the mist. In some embodiments, the method further includes controlling the air flow rate in the air separator with a controller. In some embodiments, the controller is capable of activating or deactivating the vacuum source, the air flow or a contaminated gas treatment system in fluid communication with the vacuum source. In another embodiment, a method for reducing the levels of contaminants in a contaminated liquid includes aerating the contaminated liquid in an aeration module to produce a first phase of contaminated gas, transporting the first phase of contaminated gas to one or more treatment systems, and the different levels of contaminants in the contaminated gas phase in the one or more treatment systems. In some embodiments, the method also includes collecting the contaminated liquid after aeration, wherein one or more of the contaminants in the contaminated liquid is MTBE and wherein the aeration step removes at least about 98% of the MTBE from the contaminated liquid. . In some embodiments, the aeration stage of the contaminated water removes at least approximately 99% of the MTBE from the contaminated liquid. Some embodiments of the above embodiments include filtering the contaminated liquid. In one embodiment, the method includes receiving a second phase of contaminated gas in the module of aeration of a contaminated gas source, transporting the second phase of contaminated gas in the aeration module to one or more treatment systems and reducing the contaminants in the second phase of gas contaminated with the one or more treatment systems. In some embodiments, the method includes mixing the second phase of contaminated gas with the first phase of contaminated gas. In some modalities, the source of contaminated gas is soil or soil. In one embodiment, a system includes an aerator module configured to convert one or more contaminants into a contaminated liquid into gas phase pollutants, a separator tower configured to convert the contaminated liquid to a contaminated gas phase and a liquid at reduced levels of the gas. one or more pollutants and a contaminated gas treatment system configured to receive the phase of contaminated gas and gas phase pollutants. In some embodiments, the contaminated gas treatment system reduces the level of contaminants in the contaminated gas phase and gas phase pollutants. In some embodiments, the aerator module comprises a plurality of nozzles, wherein the nozzles are configured to feed gas bubbles to the contaminated liquid. In some embodiments, the aerator module operates under a static or dynamic vacuum. In some embodiments, the separating tower comprises a high vacuum environment. In some embodiments, the separating tower comprises a plurality of nozzles that receive the contaminated liquid and is configured to convert the contaminated liquid to an atomized contaminated mist. In the previous mode, the contaminated mist is converted to the contaminated gas phase and the liquid with reduced levels of one or more pollutants. In some embodiments, the liquid with reduced levels of one or more contaminants comprises less than about 5% of the contaminants in the contaminated liquid. In some embodiments, the liquid with reduced levels of one or more contaminants comprises less than about 1% of the contaminants in the contaminated liquid. In some embodiments, the liquid with reduced levels of one or more contaminants comprises less than about 0.5% of the contaminants in the contaminated liquid. In some embodiments, the liquid with reduced levels of one or more contaminants comprises less than about 0.1% of the pollutants in the contaminated liquid. These results are further exemplified in the Tables attached to this disclosure. In some embodiments, the one or more contaminants are volatile organic compounds. In the aforementioned modality, the contaminated gas treatment system reduces contaminant levels through one or more processes selected from the group consisting of adsorption, oxidation and condensation of contaminants. In some embodiments, the aerator module, the separator tower and the contaminated gas treatment system are in communication with a controller. In some embodiments, the controller is capable of activating or deactivating one or more aerator modules, the separator tower, the contaminated gas treatment system. In some embodiments, the controller is capable of regulating one or more of the aerator module, the separator tower and the contaminated gas treatment system. The controller is capable of regulating the transfer of effluent or water effluent to or from one or more of the aerator module or the separator tower. In some embodiments, the controller is capable of regulating the flow of contaminated gas from one or more of the aerator module and the separator tower. In some embodiments, the system is configured to extract and treat a contaminated gas from the soil, where the contaminated gas does not comprise a contaminated liquid. In another embodiment, a system includes an aerator module configured to convert one or more contaminants in a contaminated liquid to gas phase contaminants and a contaminated gas treatment system configured to receive the gas phase contaminants. In this mode, the contaminated gas treatment system reduces levels of contaminants in the gas phase pollutants. In another embodiment, a system comprises a separating tower configured to convert a contaminated liquid to a contaminated gas phase and a liquid with reduced levels of one or more contaminants and a contaminated gas treatment system configured to define the contaminated gas phase. In this mode, the contaminated gas treatment system reduces the levels of contaminants in the contaminated gas phase. In this embodiment, the liquid with reduced levels of the one or more contaminants is substantially free of contaminants. In one embodiment, the separator tower receives dilution air that is mixed with the contaminated gas phase in the separator tower. In one embodiment, the contaminated gas phase treatment system is configured to control the amount of dilution air. As used herein, in any of the embodiments, the contaminated liquid may be contaminated water. In another embodiment of an apparatus for reducing the levels of one or more contaminants in contaminated water, the apparatus includes a first container configured to receive contaminated water; the container includes one or more side walls, one or more bottom walls and one or more top walls, the one or more side walls, the one or more bottom walls and one or more top walls are in contact to digest the interior of the container. In some embodiments, the container also includes a first inlet in fluid connection with a source of contaminated water, at least a second inlet in fluid connection with a gas source, a first outlet in fluid connection with a liquid transfer pump and a second output coupled to a first source of vacuum. In some embodiments, the interior is adapted to contain contaminated liquid and the second inlet is configured to feed a gas to the contaminated liquid. The apparatus may further include a tower in fluid connection with the liquid transfer pump, the tower further includes a third inlet for receiving the contaminated liquid from the liquid transfer pump, a vacuum chamber having a third outlet coupled to a second vacuum source and a plurality of nozzles in fluid connection with the third inlet. In some embodiments, the plurality of nozzles configured to feed the contaminated liquid into the vacuum chamber as an atomized liquid. In some embodiments, the tower may also include a bottom to receive a clean contaminated liquid and a fourth outlet located near the bottom to remove the clean contaminated liquid. In some embodiments, the at least one second inlet is connected to a gas manifold located at least partially inside the container, the gas manifold comprises a plurality of orifices configured for Feed air to contaminated water in the first container. In some embodiments, the contaminated water source consists of one or more means for treating water, in which one or more components described herein are included. In some modalities, the source of contaminated water is the soil. In some embodiments, the first container is a container with baffles. In some embodiments, the first container comprises a plurality of surfaces adapted to create an indirect path for contaminated water inside the container. In some embodiments, at least some of the orifices of the gas manifold are located near the one or more walls of the bottom of the container. In some embodiments, the interior of the container comprises two or more chambers, each chamber partially separated by a set of walls, wherein at least some of the walls define orifices between each chamber to allow contaminated water to pass through the two or more cameras. In some embodiments, the gas manifold has one or more orifices to create the bubbles within one or more of the chambers, the gas manifold is fluidly connected to the second inlet. In some of the above embodiments of apparatus, means for treating a contaminated gas may be included. Such treatment means in fluid connection with the third outlet of the high vacuum chamber. In some modalities, a system of contaminated gas treatment in fluid connection with the second outlet of the first container and the third outlet of the vacuum chamber. In some embodiments, the contaminated gas treatment system is one or more selected from the group consisting of an electrical catalytic oxidant, a thermal oxidant, an adsorption filtration system, a condenser, an oxidant to the flame, a treatment system Cryogenic, a gas cooling and liquefaction system, regenerative thermal oxidizers and rotating concentrators. In another embodiment, an apparatus includes a tank for holding a liquid, the tank comprises a first inlet for the transport of liquid tributary, a first outlet for the transport of liquid effluent and a second outlet for the transport of effluent from a gas contaminated, the tank further comprises a plurality of deflectors, each deflector mounted within the tank in substantially parallel positions, wherein the liquid of the first inlet is configured to travel in one or more chambers within the tank at the first outlet, each chamber separated at least one of the plurality of baffles and each chamber comprises a gas delivery system for bubbling a gas through the liquid. Some embodiments may further include a first vacuum source in fluid connection with the second tank outlet, the vacuum source configured to feed the contaminated gas to a gas treatment system. In some modalities, the apparatus includes a gas treatment system. In certain embodiments, the first source of vacuum is at least a portion of a gas treatment system. For example, in some embodiments, the gas treatment system is an electrical catalytic oxidant and the at least one portion is an oxidant blower capable of creating the vacuum source. In some embodiments, the apparatus may include an air separator in fluid connection with the first outlet, the air separator in the form of a cylindrical column, the column comprises a plurality of nozzles near the top of the column to convert the liquid in a contaminated mist, the cylindrical column has a distance from the plurality of nozzles to the bottom that allows the mist to fall gravitationally into the column, the air separator in fluid connection with a second vacuum source to create a vacuum with the column cylindrical, the air separator further comprises a second inlet connected to a second air source, the second inlet positioned in the column to allow air from the air source to pass the mist as the mist falls gravitationally into the air. column. In some embodiments, the gas treatment system in fluid connection with the first and second vacuum sources. In some embodiments, the second vacuum source is adapted to feed the contaminated gas from the separator of air to the contaminated gas in the tank. In another embodiment, an apparatus includes an air separator in fluid connection with a contaminated water source, the air separator in the form of a cylindrical column, the column comprises a plurality of nozzles near the top of the column to convert a liquid in contaminated mist, the cylindrical column has a distance from the plurality of nozzles to the bottom that allows the mist to fall gravitationally inside the column, the air separator in fluid connection with a vacuum source to create a vacuum inside the column cylindrical, the air separator further comprises a first inlet connected to an air source, the second inlet positioned in the column to allow air from the air source to pass the mist as the mist falls gravitationally into the column . In some embodiments, the air separator further includes a sump for collecting clean water that has fallen to the bottom of the column, the sump in fluid connection with a transfer pump. In some modalities, the carcass also includes a switch to detect a clean water level in the station, the switch in communication with the transfer pump and capable of activating the transfer pump to remove the clean water when it reaches the level. In one embodiment, the apparatus further includes a contaminated gas treatment system in fluid connection with the vacuum source.

In some modalities, the decontaminated liquid can be processed multiple times through the system for additional decontamination.

BRIEF DESCRIPTION OF THE FIGURES Figure 1 is a drawing of a modality that includes an aerator module, a separator tower and a contaminated gas treatment system. Figure 2 is a drawing of a mode including a separator tower and a contaminated gas treatment system. Figure 3 is a drawing of one embodiment including an aerator module and a contaminated gas treatment system. Figure 4 is a drawing of a mode including an aerator module, a filter module, a separator tower and a contaminated gas treatment system. Figure 5 is a drawing of one embodiment including an aerator module and a separator tower. Figure 6 is a drawing of one embodiment including an aerator module, two separating towers in series and a contaminated gas treatment system. Figure 7 is a schematic drawing of an aerator module. Figure 8 is a schematic drawing of a modality of an aerator module containing deflectors. Figure 8A is a detailed view of an aerator module. Figure 8B is a front view of an aerator module. Figure 8C is a side view of an aerator module. Figure 8D is a top view of an aerator module. Figure 9 is a schematic drawing of a filter module and also shows a liquid transfer pump. Figure 10 is a schematic drawing of a separator tower module. Figure 11 is a schematic drawing of arrangement of the plurality of nozzles inside the separating tower. Figure 12 is a schematic drawing of a catalytic oxidant module. Figure 13 is a schematic drawing of a condenser system. Figure 14 is a schematic drawing of an adsorption filtration system. Figure 15 is a schematic drawing of a liquid decontamination system in one configuration. Figure 16 is a top view of a liquid decontamination system in one configuration.

Figure 17 is a form of a liquid decontamination system that was integrated and tested. Figure 18 is a schematic drawing of another configuration of a liquid decontamination system.

DETAILED DESCRIPTION OF THE INVENTION Systems and methods for separating contaminants from liquids are described herein. Contaminated liquids can include water, alcohols, hydrocarbons, oils, suspensions, solutions, dissolved and melted solids or condensed gases. In certain modalities, water is the contaminated liquid. Some embodiments described herein are specifically in relation to contaminated water, but may also be applicable to many other contaminated liquids. In some modalities, contaminated water contains pollutants that are more volatile than contaminated water. For example, pollutants in contaminated water may have a boiling point that is lower than that of water. Other examples include contaminants that have a vapor pressure greater than water. The contaminants may include at least one volatile organic compound ("VOC"). For example, contaminants may include but are not limited to benzene, toluene, ethylbenzene, xylene (these four compounds are commonly referred to as BTEX); methyl-tertiary-butyl-ether (MBTE), tert-butanol (TBA), trichloroethene (TCE), Perchloroethene (PCE) and 1,4-dioxane and other contaminants described herein. Many of the pollutants are soluble in the contaminated liquid. However, contaminants may also be suspended in the contaminated liquid. Contaminants can also be immiscible with the contaminated liquid and can in many cases form an emulsion. Additionally, some embodiments of the liquid decontamination system are also capable of purifying liquid contaminated with contaminants that are solid. Contaminants can also include solids such as sediment and sand. Small particles that have a diameter greater than about 0.1, 0.2, 0.3, 0.4, 0.5, 1, 2, 5, 7, 9, 12, 15 and 20 microns can also be purified by a filtration system of the liquid decontamination system. The solids may also include larger objects and such objects may be purified from contaminated water by sieves, filters, traps and other similar means of filtering liquid solids. In another embodiment, the systems and methods as described herein are capable of purifying liquids contaminated with contaminants that are gases at standard temperature and pressure such as nitrogen. Processes such as aeration and air separation of contaminated water can in general result in the removal of dissolved gases in the contaminated phreatic water. As will be recognized by a person having skill in the art, many of the VOC contaminants are in equilibrium between their liquid and gaseous states. In certain modalities, the system and methods that employ a multi-stage process to remove various contaminants from liquids. In some of these embodiments, a system for separating contaminants from a contaminated liquid comprises one or more selected from a group consisting of an aerator module, a filtration module, a separation tower module and a contaminated gas treatment system. . These component modules of a system for separating pollutants from contaminated liquids can be used together in combination. In some embodiments, only one module is necessary to remove contaminants from the contaminated liquid. In other embodiments, two or more selected from at least one aerator module, at least one separator tower, at least one filter module and at least one contaminated gas treatment system are used to separate the contaminants from the water contaminated Referring to Figure 1, one embodiment includes an aerator module 10 in fluid connection with the separator tower 200. The aerator module is adapted to transport volatile gaseous contaminants to a contaminated treatment system 201. In addition, the aerator module 10 can also transport contaminated water to the separating tower 200, which can also separate contaminants from contaminated water and transfer those contaminants to a contaminant treatment system 201. Optionally, contaminants from the separator tower can be treated by a separate contaminated gas treatment system 202. Referring to Figure 2, one embodiment includes a separator tower 200 and a contaminated gas treatment system 201. Separator tower 200 is capable of receiving contaminated water and separating at least some contaminants from the water. The contaminated gas treatment system 201 can then receive and treat the contaminants from the separator tower 200. Referring to Figure 3, one embodiment includes an aerator module 10 and a contaminated gas treatment system 201. The aerator module is able to separate contaminants from contaminated water. The contaminated gas treatment system 201 can then receive the contaminants from the aerator module 10. Referring to Figure 4, one embodiment includes an aerator module 10, a filter module 60, a separator tower 200, and a waste treatment system. contaminated gas 201. The aerator module 10 can receive contaminated water and separate at least some contaminants from the contaminated water. The contaminated gas treatment system 201 can receive contaminants from the aerator module 10. In addition, the aerator module 10 can then transport the contaminated water through a filter module to reduce the amount of solid contaminants and the contaminated water can then be transferred to the separator tower 200. The separator tower 200 is capable of receiving contaminated water and Separate at least some contaminants from the water. The contaminants in the separator tower 200 can then be transported to the contaminated gas treatment system 201. In some embodiments, the contaminants in the separator tower 200 can be combined with some contaminants in the aerator module 10 before or during treatment by the system. treatment of contaminated gas 201. Referring to Figure 5, one embodiment includes the aerator module 10 and a separator tower 200. The contaminated water enters the aerator module 10 and is aerated resulting in contaminants exiting the aerator module 10. The water can then be transferred from the aerated module 5 to the separating tower 200. In the separating tower 200, pollutants from the contaminated water are transferred to gaseous phase pollutants leaving the separating tower. As a result, clean water can be recovered from the separator tower 200. Referring to Figure 6, one embodiment includes the aerator module 10, two or more separator towers 200 and a contaminated gas treatment system 201. In this mode, contaminated water is aerated in the aerated module, separating at least some of the contaminants. The contaminated water can be transferred to the separator tower 200, where more contaminants change phase to gas phase pollutants and the process can be repeated in the second separator tower 200. An advantage of a multi-stage system is the increased efficiency in purify pollutants from contaminated liquid. By using multiple components to purify a liquid, each component can selectively target a specific contaminant. For example, a liquid contaminated by solid particles and VOC can be purified by the use of a filter module 10 and the separator tower 200. However, in some preferred embodiments, a system comprising an aerator module 10, a module filtration 60, a separator tower module 200 and a contaminated gas treatment system 201 provide an efficient method for removing contaminants from a contaminated liquid. In certain embodiments, the same contaminant is purified in more than one component of the liquid purification system. A general description of a process using an aerator 10, filter 60, separator tower 200 and contaminated gas treatment system 201 is provided below. A contaminated liquid can be introduced into an aeration tank 10 comprising an aeration compressor 20. Such aeration compressor 20 operates to produce small bubbles that rise through the contaminated liquid to the upper space 12 of the aeration tank 10. Bubbles introduced to the contaminated liquid carry contaminants of contaminated liquid to the upper space 12 of the aeration tank 10. Additionally, an aeration tank 11 may comprise deflectors to create a more tortuous path for the bubbles and to expose the bubbles to more surface area. In turn, such a method would result in increased efficiency in the removal of contaminants by the aerator module 10. These contaminants are then transferred out of the aeration tank 10 with the contaminated air and processed by the contaminated gas treatment system 201. In some embodiments, the aerator module operates under biostatic or dynamic pumps to prevent the exit of contaminants. The contaminated gas treatment system 201 can release the stream of purified gas as environmentally safe exhaust to the atmosphere or can otherwise trap the contaminants. In some embodiments, liquids that have been processed by the reactor module 10 can be transferred to one or more other treatment modules 201, 202. In one embodiment, the contaminated liquid can be transferred to at least one filter module 60. In some embodiments, a liquid transfer pump is used to transfer liquid from the aerator module 10 to a filter 60. In one embodiment, the filter module comprises a bag filter housing. In another embodiment, the filter module comprises two bag filter housings arranged in series. The bag filter housings are capable of removing solids that are contaminants and / or those solids that could potentially foul equipment downstream of the filter. Optionally, the filter numbers 60 can be placed before the aerator module 10 as both before and after the aerator module 10. In some embodiments, the contaminated liquid can be transferred to a separator tower module 200. In some embodiments of this module, the liquid enters a warm vacuum chamber through at least one atomization nozzle. The liquid is thus converted into a mist. The vacuum environment converts the contaminated liquid mist to a contaminated gas phase and a liquid fog phase. Pressure inside such a chamber may vary, but includes from about 20 inches of HgG to about 30 inches of HgG and more preferably of about 26 inches of HgG. In one embodiment, the pressure is approximately 2 PSIA. The vacuum environment can be adjusted depending on the contaminants and the liquid to be decontaminated can thus be less than 20 inches or greater than 30 inches of HgG. An example of a vacuum pump that can be used in the vacuum pump unit have 2 ML -8.3 HP. Then the contaminated gas phase can be transported far away by the vacuum pump. Additionally, the liquid mist may pass over the optional random pass, thus exposing the mist to more surface area within the separation tower 200. To assist in the removal of the gas phase contaminants, carrier air may be added to the tower Separator 200. To assist in the removal of gas phase contaminants, carrier air can be added to the separator tower 200. The carrier air passes over the packaging material that has exposed the most surface area of the liquid mist, thereby removing any remaining contaminants from the liquid fog phase. Then the dilution air comprising the contaminants is transported to the vacuum pump. In some embodiments, the rate and amount of dilution air can be controlled to increase the removal efficiency of contaminants from the contaminated water in the separator tower 200. The liquid mist can be collected in drops of liquid. These drops can be collected in the bottom portion of the separating tower (also known as the sump). The liquid can be pumped from the separator tower to a storage tank. In some modalities, the liquid can be taken directly from the separating tower.

Such a liquid may be subjected to one or more other treatment means, in which the modules are included as described herein. In some embodiments, the liquid may contain less than 10% of the target contaminants of contaminated liquid. In some embodiments, the decontaminated liquid comprises less than about 5%, 4.5%, 4%, 3.5%, 3%, 2.5%, 2%, 1.5%, 1% of the target contaminants of contaminated liquid. In preferred embodiments, the purified liquid contains less than 1% of the target contaminants in which are included approximately 0.0001%, 0.001%, 0.01%, 0.5%, 0.1% and 0.5% and values among the above. In some embodiments, the contaminated gas phase and the carrier air (also referred to herein as the dilution air) are transported away from the separator tower. In some embodiments, these gases pass through the process gas blower. Optionally, contaminants can also pass through a contaminated gas treatment system. Such systems are described further herein. The modules and certain modalities are described below as they relate to the attached Figures. However, this is not intended in any way to limit the scope of the invention which is defined by the claims that follow.

Aerator Module Figure 7 represents a non-limiting example of an aerator module 10. The contaminated liquid 13 enters the aeration tank 11 at the liquid tributary connection point 15. The connection point of the liquid effluent of the contaminated liquid 15 is located above the level of static contaminated liquid in the aeration tank 10. However, in some embodiments, the liquid tributary connection point 15 may be connected to another location within the aeration tank 11. In some embodiments, the tributary connection point 15 is located above the contaminated water level 13. This sale permits the polluted water 13 to be treated by the aerator module 10 and transported away from the aeration tank 11 in the course of connection of effluent 45. In some embodiments, the contaminated water 13 may be connected to the aeration tank 11 to further increase the efficiency of removing r contaminants of contaminated water 13. The aeration tank 11 is in communication with the aeration compressor 20. The aeration compressor 20 is configured to feed compressed gases to the aeration tank 11 by means of a gas distribution manifold 25. In some embodiments, the aeration compressor 20 continuously feeds air or other gases to the gas distribution manifold 25. It can provide the gases selected, such as air to contaminated water 13 at a pressure sufficient to effect the bubbling in the contaminated water 13 in the aerator tank 11. In some embodiments, the air can be fed to the aeration tank 11 by a source of compressed air. In some embodiments, gases such as ozone can be used in the purification of water during the aeration process. In some embodiments, the aeration module 10 may also comprise a ultraviolet light purification system. In some embodiments, the air filter 60 is used to purify the incoming air from the air compressor 20. In some embodiments, the gas distribution manifold 25 can be attached to the bottom of the aeration tank 11. The aeration compressor 20 is connected to the aeration tank 11 via the pipe 66. The pipe 66 is connected to the gas inflow connection bottom 55 near the base of the aeration tank 11. The gas distribution manifold 25 can be connected additionally to the pipe 66 to the gas tributary connection point 55. In some embodiments, the pipe 66 is equipped with a check valve 65, manual ball valve 70 and a pressure gauge 75. The check valve 65 is designed to prevent the flow of gas from the tank of aeration 11 back through the aeration compressor 20. If the manual ball valve 70 is closed it allows the service of the aeration compressor 20 and the check valve 65. The gauge 75 indicates the pressure of clean air entering the aeration tank 11. The manual ball valve 70 allows the manometer 75 to be serviced. The gas distribution manifold 25 can comprise a plurality of pipes extending the length of the tank of aeration 11. The gas distribution manifold 25 may be attached to the bottom of the aeration tank 10 or be configured to be close to the bottom of the aeration tank 11. In some embodiments, the gas distribution manifold 25 comprises a plurality of registers 30. In some embodiments, the gas distribution manifold is drilled with holes several times per inch. The size of the holes may vary depending on the fixation and pressure. In one embodiment, the holes are generally of small diameter. Since the gas distribution manifold 25 is pressurized by the aeration compressor 20, the gas leaves the clean air distribution manifold 25 through the orifices 30. The orifices 30 cause the gases, such as compressed air, to form small bubbles as the clean air leaves the air distribution manifold 25 and enters the aeration tank 11. The small bubbles exit the clean air distribution manifold 25 and rise through the contaminated liquid 13 in the tank. aeration 11. As the bubbles rise through the contaminated liquid 13, some of the contaminant is transferred from the liquid polluted to the bubbles. The aeration tank 11 can be manufactured in different sizes, shapes and materials. In one embodiment, the aeration tank 11 may be constructed of stainless steel or other suitable materials to contain the contaminated water 13. In some embodiments, the aeration tank 11 may contain up to 3785 liters (1000 gallons) of contaminated water, in the which include approximately 189 liters (50 gallons), 378 liters (100 gallons), 757 liters (200 gallons), 1135 liters (300 gallons), 1514 liters (400 gallons), 1892 liters (500 gallons), 2271 liters (600 gallons), 2649 liters (700 gallons), 3028 liters (800 gallons), 3406 liters (900 gallons) and 3785 liters (1000 gallons). Intervals between, below and above such gallon values are also contemplated. With respect to Figure 8, in some embodiments, the aeration tank 11 contains a series of internal walls or baffles 23. The contaminated liquid 13 enters the tank 11 at the point of tributary connection 15 and flows above and below the wall , which creates a tortuous path for water. The tortuous path increases the resistance time of the contaminated liquid 13 in the aeration tank 11. The increase in residence time allows more contaminant in the liquid to be transferred to the bubbles generated by the aeration compressor 20 and the distribution manifold gas 25. Then the pollutants are transferred to the upper space 19 of the tank 11. This is a method to increase the amount of contaminants that can be transferred from the liquid phase to the gas phase while they are in the aeration tank 11. Once these contaminants are in the phase Soda is removed from the aeration tank 11 and destroyed by a contaminated gas treatment system. Additionally, in some modalities, walls are added to the aerator module to make the trajectory for the most tortuous bubbles, thereby increasing the residence time. When the bubbles reach the next contaminated liquid, they accumulate in the upper space 19 above the aeration tank 11. The aeration tank 11 can be equipped with an air tight cover 14 to prevent gaseous contaminants from escaping into the atmosphere. In one embodiment, the upper space 19 is connected to a vacuum pump. In another embodiment, the upper space 19 of the aeration tank 11 is connected to the negative pressure side of the process gas blower 510 via a pipe. The pipe is equipped with an automatic vacuum control valve 51. The automatic vacuum control valve 51 ensures that a steady state vacuum is maintained in the upper space 19 of the aeration tank 11. In some embodiments, the gaseous pollutants travel to a contaminated gas phase treatment system 201. The phase treatment system of contaminated gas can be specifically intended to oxidize, adsorb and / or condense the target contaminants in the gas phase. Such gas phase treatment systems are further described herein. Other means to increase the residence time of the bubbles and the efficiency of the aerator tank can also be used. In another embodiment, the aeration tank or the water inside the aeration tank can be heated. Without wishing to be limited to any particular theory, heating the aeration tank or the water inside the aeration tank can increase the efficiency of the overall process of decontaminating the water. In some embodiments, a heat interleaver may be used to heat the contaminated liquid 13 before, during or after the aeration tank module. In some particular embodiments, the heat interleaver can exchange the heat of ignition with another component of the liquid decontamination system. For example, a heat exchanger can exchange heat from one or more of the contaminant treatment system, the vacuum pump or the liquid transfer pump. In some embodiments, a heat exchanger may be a water to water heat exchanger, air to water heat exchanger, water to air heat exchanger or air to air heat exchanger. In some modalities, the water is heated to a temperature that ranges from about 10 ° C (50 ° F) to about 40.5 ° C (105 ° F). In another embodiment, the water is heated to a temperature ranging from about 27 ° C (80 ° F) to about 38 ° C (100 ° F). In addition, the vacuum pressure maintained in the aeration tank can also be controlled. In some modalities, the vacuum pressure is static and produces a vacuum. In some modalities, the vacuum is dynamic. In some embodiments, the pressure is less than the atmospheric pressure. In some embodiments, the pressure is approximately 680 to 780 Torr. In some embodiments, the pressure is from about 740 to about 760 Torr. In some embodiments, the vacuum pressure is dependent on the temperature of the contaminated liquid 13. In one embodiment, the aeration tank 11 will receive contaminated gases directly from a contaminated source. These gases may or may not be dissolved in a contaminated liquid 13. For example, it will be understood by those of ordinary skill in the art that the liquid decontamination systems described herein may operate in a double phase capacity. As such, the contaminated gases fed to the aeration module 10 or any other water decontamination system module, can pass directly to the contaminated gas treatment system 201 by means of feeding means as described herein. In one embodiment, the effluent connection inlet is configured above the level of contaminated water, such that the contaminated gases, which are fed to the aeration module, pass directly into the upper space 19 of the aeration tank 10. From the space upper 19, the contaminated gas phase can be bounded to the contaminated gas treatment system 201 via vacuum or other means. In some embodiments, the aeration module 10 can be put into continuous operation and / or automatically. In one embodiment, the aeration tank 11 is equipped with liquid level control 35 and a high level alarm closing switch 85. As the contaminated liquid fills the aeration tank 11, the level of contaminated liquid is monitored continuously by controlling the liquid level. At a level of contaminated liquid adjustable in the field, the liquid level control 35 is activated and sends a start signal from the pump to a programmable logic controller in a control panel. Then the programmable logic controller sends a signal to start the contaminated liquid transfer pump 90. While the foregoing is described as a programmable logic controller, other manual and automatic means of signaling the transfer pump are known and contemplated herein. Such automated systems are also described further in the I presented . In one embodiment, the contaminated liquid transfer pump 90 starts and pumps the contaminated liquid 13 away from the aerator tank 11. The contaminated liquid transfer pump 90 can pump the contaminated liquid to one or more other modules of the waste system. decontamination of water, such as the filtration system or the separating tower. If the contaminated liquid transfer pump 90 fails to start or fails to prime, if the aeration tank 10 is filling too quickly, the level of contaminated liquid will continue to rise in the aeration tank 10. The level of contaminated liquid that is Elevation in the aeration tank 10 will inevitably reach the high-level alarm float switch 85. At the high level alarm point, the high level alarm float switch 85 is activated and sends a signal to the programmable logic controller in the control panel. Then the programmable logic controller closes the system and defines the flow of contaminated liquid to the aeration tank 10. Figure 8A shows a detailed view of a configuration of an aerator module. The aerator tank 11 is composed of four side walls 391A, 391B, 391C, 291D and a bottom wall 392. The walls can be joined together by any means to form a box, which include but are not limited to, welded together on the respective sides of each wall. The side wall 391C includes an affluent connection point 15 in which the contaminated water is allowed to pass into the aeration tank 11. The side wall 391A includes the effluent connection point 45 in which the contaminated water is allowed to pass through it. away from the aeration tank. The side wall 291B includes opening the contaminated gas effluent connection point 50. The side wall 291B may be equipped with drain valves 397 to allow drainage of the aeration tank 11. Placed inside the tank formed by the side walls 391A- D and the bottom wall 392 is the gas distribution manifold 25. The gas distribution manifold 25 includes a gas affluent connection point 55, which can be connected to an air compressor and another gas management system. gas. The gas distribution manifold comprises a plurality of holes 30, which are nipples of 0.5 inches. However, as discussed above, the size of the holes 30 may vary. Also within the aeration tank are baffles 23A, 23B, 23C, 23D and 23E. These deflectors create a tortuous path for the water as it enters the aeration tank 11. As shown, some baffles, such as baffles 23B, 23D and 23E may contain holes 399, 398 for water to pass through as water fills each respective chamber of the aeration tank. Alternatively, deflectors, such as deflectors 23A and 23C may be oriented to allow water to pass under the deflectors. The orientation of the respective chambers is shown further in Figure 8B. As previously indicated, the aeration tank 11 can operate under vacuum. The flange 394 can be welded to the side walls 391A, 391B, 391C and 391D. In some embodiments, the flange can also be welded to baffles 23A, 23B, 23C and 23D. The airtight cover 14 can be spliced to the flange 394. In some embodiments, the air tight cover 14 is made of steel. In addition, in some embodiments, the bottom wall 392 may be attached to the flange 395, which is then further connected to the base 396. The base 396 allows the aeration tank not to be placed on the floor. The base 396 also includes slots 401 that allow the aeration tank 11 to be moved easily by the equipment that can manipulate the base using slots, such as a forklift. As an illustration, the water entering the aeration tank 11 at the tributary connection point 15 must pass under the deflector 23A. At the same time, the compressed air can be pumped to the aeration tank 11 via the manifold 25 and orifices 30. As the water fills the tank 11 of the Affluent connection assembly 15, the water will rise to a level such that it reaches the height of the holes 399 in the baffle 23B. The water will then fill the next chamber of the aeration tank and then it will be placed under the deflector 23C and to the next chamber. The level of the water will then rise to the height of the holes 399 of the baffle 23D and will pass through the holes 399 of the baffle 23D. After passing through the deflector 23D, the water must then fill the next chamber before it reaches the orifice 398. As shown in the figure, the water will then fill the final chamber of the aeration tank 11. The water can then be removed by means of the effluent connection point 45 in the side wall 391A. In some embodiments, the last chamber may be equipped with a float switch or other mechanism that automates the liquid transfer pump 90 and removes the contaminated water via the liquid effluent connection bottom 45. Figure 8B presents a view front of the aeration tank of Figure 8A. As shown, the aeration pad can be divided into multiple chambers by deflectors 23A, 23B, 23C, 23D and 23F. As shown, the deflectors 23A and 23C are not connected to the bottom wall 392, which allows the water to pass under the deflectors 23A and 23C. As shown further, the deflectors 23B, 23C, 23D are brought into contact with the bottom wall 392 and top cover 14, allowing water to pass only through the holes in the respective baffle. The gas distribution manifold 25 can be configured to pass through each respective baffle in a different orifice as the water passes. In addition, the gas distribution manifold 25 has a number of episodes that feed air to the respective chambers through the orifices 30. Referring to Figure 8B, the chambers as defined by the deflectors 23A, 23B, 23C and 23D . The cameras can be of the same or different sizes. In one embodiment, each of the lengths a, b, c, d, e and f fluctuates independently from about 15 cm (6 inches) to about 102 cm (40 inches). In one embodiment, each length a, b and e is approximately 30 cm (12 inches), each length c is approximately 46 cm (18 inches), the length e is approximately 65.5 cm (25.8 inches). However, these lengths may vary according to the size, dimensions and flow rates desired of the contaminated water. The height g can range from about 76 cm (30 inches) to about 152 cm (60 inches). In some embodiments, the height g is approximately 127 cm (50 inches). Referring to Figure 8C, this side view of the aerator tank 11 shows the manifold 25 that feeds air through the holes 30. It also shows holes 399 in a baffle In some embodiments, the length i ranges from approximately 50 cm (20 inches) to approximately 102 cm (40 inches), which include approximately 63 cm (25 inches), 66 cm (26 inches), 69 cm (27 inches) ), 71 cm (28 inches), 74 cm (29 inches), 76 cm (30 inches), 79 cm (31 inches) and 81 cm (32 inches) In addition, a top view of the shifter 11 is shown on the Figure 8D The length h can range from about 203 cm (80 inches) to about 381 cm (150 inches) In some embodiments, the length h ranges from about 203 cm (80 inches) to about 305 cm (120 inches). In one embodiment, the length h is approximately 254 cm (100 inches).

Transfer Pump and Filter Module As discussed above, some embodiments of the systems may include a transfer pump 90 to transfer contaminated water from one component to another. Referring to Figure 9, in one embodiment, the transfer pump 90 can transfer contaminated water from the aeration module 10 to a filtration module 300. The contaminated liquid transfer pump 90 can be connected to the aeration tank 10 via the pipeline 107. In one embodiment, the pipe 107 is connected to the aeration tank 10 near the bottom of the final chamber at the effluent connection point 45.

In some embodiments, the tubing may be equipped with ball valves 105 and 110 and strainer and 120 positioned on the upstream side of the contaminated liquid transfer pump 90. The closing of the ball valves 105 and 110 allows serving the strainer and 120. The strainer y 120 is designed to remove solid particles larger than 20 micras of contaminated liquid. However, other filters can be used in place of the colander and 120. In some embodiments, no filter is necessary because the contaminated water was prefiltered. The filtered water prevents damage to the contaminated liquid transfer pump 90. However, the filter sizes may vary and solid particles may be greater than or less than about 20 microns, which include about 5, about 10 and about 15. Chips can be removed. The contaminated liquid transfer pump 90 can be any type of pump. In one embodiment, the contaminated liquid transfer pump 90 is a centrifugal pump. To obtain continuous flows, a 5 horsepower pump can be used for the system of 37.8 liters / minute - 57 liters / minute (10-15 gallons per minute). A larger pump can be used in a system with increased flow rates and production rates of water. Thus, the size and power of the transfer pump Contaminated liquid can vary according to the total output of the liquid decontamination system. An example of an appropriate transfer pump is the 1.5 HP, TEFC, three-phase transfer pump, available from Price Pump Co. (Part No. CD100BF-450-6A212-150-353T6). Other suitable transfer pumps include Gould Pumps (G and L Model Series NPR / NPE-F), available from ITT Water Technology, Inc. The appropriate liquid transfer pumps can increase the water pressure to an amount of approximately 14.1 Kg / cm2 (absolute) 200 psia (pounds / square inch absolute), which includes pressures of approximately 0.35 Kg / cm2 (absolute) (5 psia), 0.70 Kg / cm2 (absolute) (10 psia), 1.0 Kg / cm2 (absolute) (15 psia), 1.4 Kg / cm2 (absolute) (20 psia), 1.76 Kg / cm2 (absolute) (25 psia), 2.1 Kg / cm2 (absolute) (30 psia), 2.5 Kg / cm2 (absolute ) (35 psia), 2.8 Kg / cm2 (absolute) (40 psia), 3.2 Kg / cm2 (absolute) (45 psia), 3.5 Kg / cm2 (absolute) (50 psia), 3.9 Kg / cm2 (absolute) ( 55 psia), 4.2 Kg / cm2 (absolute) (60 psia), 4.6 Kg / cm2 (absolute) (65 psia), 4.9 Kg / cm2 (absolute) (70 psia), 5.3 Kg / cm2 (absolute) (75 psia) ), 5.6 Kg / cm2 (absolute) (80 psia), 6.0 Kg / cm2 (absolute) (85 psia), 6.3 Kg / cm2 (absolute) (90 psia), 6.7 Kg / cm2 (absolut) uta) (95 psia), 7.03 Kg / cm2 (absolute) (100 psia), 7.38 Kg / cm2 (absolute) (105 psia), 7.7 Kg / cm2 (absolute) (110 psia), 8.1 Kg / cm2 (absolute) (115 psia), 8.4 Kg / cm2 (absolute) (120 psia), 8.8 Kg / cm2 (absolute) (125 psia), 9.1 Kg / cm2 (absolute) (130 psia), 9.5 Kg / cm2 (absolute) (135 psia), 9.8 Kg / cm2 (absolute) (140 psia), 10.2 Kg / cm2 (absolute) (145 psia) , 10.5 Kg / cm2 (absolute) (150 psia), 10.9 Kg / cm2 (absolute) (155 psia), 11.2 Kg / cm2 (absolute) (160 psia), 11.6 Kg / cm2 (absolute) (165 psia), 12.0 Kg / cm2 (absolute) (170 psia), 12.3 Kg / cm2 (absolute) (175 psia), 12.7 Kg / cm2 (absolute) (180 psia), 13.0 Kg / cm2 (absolute) (185 psia), 13.3 Kg / cm2 (absolute) (190 psia), 13.7 Kg / cm2 (absolute) (195 psia) and 14.1 Kg / cm2 (absolute) (200 psia). The pressure also includes intervals between the previous values. As used in the present "psia" means pressure per square inch, absolute is at 0 ° K. In one embodiment, the ball valves 110 and 125 are located upstream and downstream of the contaminated liquid transfer pump 90 to allow service of the contaminated liquid transfer pump 90. Referring further to Figure 9, the pump 90 of transfer of contaminated liquid is connected to the separating tower 200 by means of a pipe. As shown in the embodiment of the figures, the pipe is equipped with four ball valves 125, 130, 135, 140, a check valve 145, three sampling gates 150, 155 and 160, three pressure gauges 165, 170 and 175 and two filter housings 180 and 190. The check valve 145 is designed to prevent the backward flow of the liquid from the separating tower 200 to the aeration tank 10. The ball valves 125 and 130 allow service to the check valve 145. As further indicated in Figure 9, the contaminated liquid transfer pump 90 it can transfer the contaminated water 13 to a filtration module 300. The filtration module 300 can include one or more filters to reduce pollutants from the contaminated water. In some embodiments, the filtration module may be equipped with at least one filter housing. In other embodiments, the filter module is equipped with more than two filter housings. These filter housings can be used in series or can be used separately for two different water sources. A non-limiting example of a filtration module is shown in Figure 9. In this example, the filtration module includes the primary filter housing 180 and secondary filter housing 190. Each primary filter housing 180 and secondary filter housing 190 It can include a solid filter element. In some embodiments, each of the primary filter housing 180 and secondary filter housing 190 may be equipped with a filter element of about 5 to about 25 microns. In one embodiment, the primary filter element 180 is equipped with a 10 micron filter element and the secondary filter housing 190 is equipped with a micron filter element. In some embodiments, filters can filter particles of different sizes or the same size. The particles that can be filtered include particles having a size greater than or equal to about 1, 2, 3, 4, 5, 6, 7, 8, 9 or 10 microns. An example of suitable filters and filter housings include the cartridge filter housing and NCO model available from Rosedale Products, Inc. (Part No. NC08-15-2P - * - 150-C-V-PB). Referring to Figure 9, some embodiments include ball valves 130 and 135 that allow servicing the primary filter housing 180 and ball valves 135 and 140 that are upstream and downstream of the secondary filter housing 190. In some embodiments, gauges 165 and 170 are used to determine the service interval of the bag filter elements in the primary filter housing 180 and pressure gauges 170 and 175 to determine the service interval of the bag filter element in the secondary filter housing. The difference between the upstream and downstream gauge readings indicates the conduction of the bag filter element in the primary filter housing 180. The ball valves 205, 210 allow servicing of the gauges. Ball valves 135, 140 allow service to the secondary filter housing 180. Valves 140 and 235 allow to service 175. Referring still to Figure 9, some embodiments include sampling gates 150, 155 and 160. In these embodiments, the sampling gates 150, 155, 160 allow the collection of contaminated liquid samples. Such samples are used to determine the effectiveness of the system and process. In addition, the filtration system 300 may be equipped with a contaminated liquid temperature gauge 220 and a contaminated liquid flow meter 230. The ball valves 235 and 240 allow service to the contaminated liquid flow meter 230.

Separator Tower Module An effective way to remove contaminants such as VOC or halogenated organic compounds from water is by means of an air separation process. In some embodiments, the water decontamination system includes a separator tower module 200. In some embodiments, the separator tower 200 acts as an air separator that produces a phase change of contaminants that are dissolved in the contaminated water. At least some of the pollutants in the contaminated water change phase from liquid to gases in the separator tower 200. In some embodiments, the contaminated liquid is pumped to the separator tower 200 near the upper part of the separating tower 200. Atomizing nozzles 260 create small drops of contaminated liquid that increase the amount of surface area of contaminated liquid exposed to the dilution air. Then the atomized contaminated liquid is exposed to reduced pressures in the separation tower 200 and the contaminants change from liquid phase to gas. As the small droplets and contaminated liquid fall into the separating tower 200, the contaminants change phase. Referring to Figure 10, in some embodiments, the contaminated water is atomized through a plurality of atomization nozzles 260 in the separator tower 200 which is under vacuum. The plurality of atomization nozzles 260 may comprise atomization nozzles. The atomization nozzles 260 may be configured and arranged to provide efficient conversion of contaminated liquid to a contaminated mist. For example, Figure 11 demonstrates an array of atomization nozzles 260 in the separator tower 200. The atomization nozzles 260 are arranged on a manifold of atomization nozzles 261. In some embodiments, the manifold atomization nozzles are in fluid connection. with affluent connection point 250. The manifold of atomization nozzles can come in many different configurations. In one embodiment, the manifold of nozzles of Atomization comprising the plurality of nozzle can be located on a cartridge. Such a cartridge may be replaceable in the separator tower 200. In some embodiments, the separator tower 200 comprises approximately 20 to approximately 40 atomization nozzles 260. In some embodiments, the separator tower 200 comprises approximately 10 to approximately 50 atomization nozzles 260. In some embodiments, the atomization nozzles 260 are located near the top of the spacer tower 200 and equally spaced from each other. Suitable spray nozzles 260 include nozzles that include a size of about 4 to about 5 microns. However, the size is variable as indicated above and is not limited to the sizes described and also includes nozzles of size from about one to about 5 microns and nozzles of size from about 5 to about 20 microns. The pressure of the atomized contaminated water in the plurality of nozzles can be varied according to the flow velocity of the contaminated water, the number of nozzles and the size of the orifices of the nozzles. In some embodiments, the fluid pressure in the nozzles is between approximately 0.7 Kg / cm2 (gauge) (10 psig) (pounds / square inch gauge)) at approximately 10.5 Kg / cm2 (gauge) (150 psig). In some modalities, the Nozzle fluid pressure is between approximately 1.4 Kg / cm2 (gauge) (20 psig) to approximately 5.6 Kg / cm2 (gauge) (80 psig). In some embodiments, the fluid pressure at the nozzles is between about 2.8 Kg / cm 2 (gauge) (40 psig) to about 4.6 Kg / cm 2 (gauge) (65 psig). In some embodiments, the nozzles 260 of the separator tower 200 can optionally be heated. Methods for providing heat to spray nozzles 260 are known in the art. One method comprises providing electricity to the nozzles as long as the nozzles 260 are connected to ground to eliminate any charge. The nozzles can also be attached to a thermocouple to control the heating of the nozzles. In one embodiment, a vacuum pump 510 is adapted to be connected to the separator tower 200 near the top of the separator tower 200 at the effluent connection 475. In one embodiment, the atomization nozzles may be placed at a level below of the vacuum inlet 475. In a preferred embodiment, the vacuum inlet 475 is from about 5 cm (2 inches) to about 18 cm (7 inches) below the top of the separator tower. In this embodiment, the atomization nozzles are approximately 5 cm (2 inches) to approximately 25 cm (10 inches) below the vacuum inlet. In some In this case, the atomization nozzles can also be located below the vacuum inlet at the prescribed intervals. In some embodiments, a static or dynamic vacuum is maintained within the separator tower 200 by the vacuum pump 510. In one embodiment, a dynamic pump is preferred. A high vacuum can reduce the pressure of the separator tower module 200 to provide a high-vacuum, low-energy environment to assist in the interface transfer of the contaminants. The reduced pressures of the separator tower 200 increase the volatility of the contaminants in the contaminated area. For some embodiments, the separating tower 200 is put into operation under a high vacuum. The exact pressure of the cameras can vary depending on the contaminants. In some embodiments, the pressure is approximately 69 cm (27 inches) of Hg, but this may vary. In some embodiments, the pressure is about 2.5 cm (1 inch) to about 102 cm (40 inches) of Hg. In some modalities, the separating tower operates under a high vacuum. Referring to Figure 10, the ball valve 415 can be manipulated to obtain the proper operating pressure of the separation tower 200 in the pressure gauge 263. The pressure gauge 263 can also be automatically controlled by a programmable logic controller in the control panel or read manually.

In some embodiments, carrier air or dilution air can be passed over the contaminants to transfer many of the contaminants from the liquid phase to the gas phase. The contaminated gas phase can be mixed with the dilution air before, during or after the phase change of the gaseous pollutants. In some embodiments, the dilution air velocity can be controlled by increasing the efficiency of the transfer of contaminants from the liquid phase to the gas phase. In some embodiments, the dilution air flow rate may be varied from about 0.0142 m3 / minute (0.1 SCFM) to about 0.0425 m3 / minute (20 SCFM). In some embodiments, the dilution air flow rate can be varied from about 0.0142 m3 / minute (0.5 SCFM) to about 0.0425 m3 / minute (15 SCFM). In some embodiments, the dilution air flow rate may be varied from about 0.028 m3 / minute (1 SCFM) to about 0.28 m3 / minute (10 SCFM). The dilution air can be maintained at any flow velocity value between the ranges mentioned above. The term "SCFM" means Standard Cubic Feet per Minute, referred to pressure, a temperature and relative unit pre-specified. As used herein, SCFM is referred to 1 Kg / cm2 (14.7 psia), 20 ° C (68 ° F) and 0% relative humidity. Alternatively, in some embodiments, dilution air is not required to effect the transfer of the pollutants from the liquid phase to the gas phase. Referring to Figure 10, in one embodiment, the dilution air enters the separator tower 200 in the dilution air filter 410. The dilution air flow rate can be controlled manually or automatically. For example, the dilution air can be controlled by a programmable logic controller in the control panel. In some embodiments, the ball valve 420 is used to control the flow of dilution air entering the separator tower 200. In one embodiment, the dilution air enters the separator tower 200 near the midpoint of the carcase 280. However, other embodiments allow the dilution air to enter the separating tower at other locations in the carcase 280 or above the carcase 280. The dilution air flows through the carcase 280, optional random packing 270 and is mixed with the phase of contaminated gas. Once the dilution air is mixed with the contaminated gas phase, the mixture continues upwards in the separator tower 200 to the connection 475 of the process gas effluent. After leaving the separation tower 200, the process gas passes through the vacuum pump 510 and the process gas fan enters the contaminated gas phase treatment system 201. In some embodiments, the residence time of the atomized contaminated water can be increased by filling the separator tower 200 with optional random packing 270. The random packing 270 increases the amount of surface area within the separating tower 200. One or more supports can be used in the separating tower to support such packing material. Random packaging support grids 285 can be installed to prevent random packing from falling to the carcass 280 of the separating tower. Examples of appropriate packaging include Jaeger Tri-Packs®, but are not limited to it. In some modalities, packaging is not used. In some embodiments, the contaminated water can be heated to further increase the phase change efficiency of the contaminants in the separator tower. In some embodiments, the water can be heated by the atomization nozzles. In other embodiments, the water is heated before entering the separator tower 200. In some embodiments, the water is heated from the heat of other components of the water decontamination system, such as a heat exchanger on one of the transfer pump (for example, transfer pump 90), vacuum pump 510 or contaminated gas treatment system 201. In some embodiments, the temperature of the contaminated water must be maintained in the range of approximately 4 ° C (40 ° F). at approximately 65.5 ° C (150 ° F). In some embodiments, the temperature of the contaminated water may be maintained in the range of about 15.5 ° C (60 ° F) to about 43.3 ° C (110 ° F). In some embodiments, the temperature of the contaminated water can be maintained in the range of about 21 ° C (70 ° F) to about 43 ° C (110 ° F). As indicated above, the dimension of the separator tower module can vary with the type, amount and concentration of the contaminant (s), the volume of water to be processed by the separator tower, the desired flow velocities through the device and the desired pressures in the vacuum chamber of the separating tower. In some non-limiting modes, the separating tower is cylindrical. In some embodiments, the separating tower has a storage capacity of approximately 76 liters (20 gallons) to approximately 18925 liters (5000 gallons) of liquid. In some embodiments, the storage capacity of the separating tower is approximately 378 liters (100 gallons) to approximately 3785 liters (1000 gallons). In another embodiment, the storage capacity of the separating tower is approximately 303 liters (80 gallons) to approximately 757 liters (200 gallons). In a preferred embodiment, the separating tower has a capacity of approximately 378 liters (100 gallons). The shape and dimensions of the separating tower can vary. In one embodiment, a separating tower module Cylindrical is about one meter to about 6 meters (3 to about 20 feet). In another embodiment, the separating tower is approximately 2 meters to approximately 10 meters (6 to approximately 30 feet) high. In a preferred embodiment, the spacer tower is approximately 3.6 m (12 ft) high. Since the separation process occurs in the separator tower 200, the purified water comprising less contaminants than the contaminated water falls to the bottom of the separator tower 200. In some embodiments, the clean water can be produced at a rate of between about 3.8 liters (1 gallon) to approximately 7.6 liters (2 gallons) per minute (gpm). In some embodiments, clean water is produced at a rate of approximately 19 liters (5 gallons) to approximately 57 liters / minute (15 gallons / minute). In some embodiments, clean water is produced at a rate of approximately 38 liters / minute (10 gallons / minute). However, different configurations and scales of the liquid decontamination system can allow the production of water at speeds of 38 liters / minute (10 gpm), in which up to approximately 757 liters / minute (200 gpm) are included. In some embodiments, the clean water is collected and begins to fill the carcass 280. The carcase 280 can be filled and / or drained. This process can occur continuously or in a batch process. This process can also occur manually or automatically. In some embodiments, the carcass 280 may be equipped with a manual drain valve 315 to drain clean water from the carcass. In other embodiments, the effluent connection 320 of clean water is connected near the carcase 280. The connection 320 of the clean water effluent is connected to the clean liquid transfer pump 310 via a line 281. In some embodiments, the carcase 280 of the separator tower 200 may be equipped with a pump float switch 290 and a high liquid alarm float switch 295. The level of the liquid in elevation in the station 280 is monitored by the downstream pump float switch 290 which can be monitored manually or automatically. In one embodiment, the float switch is activated at a clean mountable water level and sends a start signal to the clean water transfer pump 410. These switches and pumps can be monitored and / or activated by some programmable logic controller in the control panel. If the clean water transfer pump 310 fails to start, fails to purge or fails to pump, the clean liquid level continues to be washed in the sump of the separator tower 280, and the level of the clean liquid will eventually reach the alarm point of high level 295. At the high-level alarm point 295, the float switch of High level alarm is activated and sends a signal to the programmable logic controller in the control panel to turn off at least part of the process. In some embodiments, the line 281 is equipped with one or more ball valves 325, 330, 335, 340, 345, 350, one or more strainers and 355 and one or more pressure valves 360, 361, one or more gates of sampling 370 and one or more clean water flow meters 380. The colander and 395 can be used to remove solid particles, which include those larger than 20 microns. The ball valves 325 and 330 allow service to the strainer and 355. The check valve 360 is designed to prevent clean water from flowing back to the separator tower 200. The check valve 365 is designed to prevent the clean liquid flow back to the clean water transfer pump 310. The ball valves 330 and 335 allow servicing of the check valve 360. The ball valves 335 and 340 allow servicing of the clean water transfer pump 310. The ball valves 3401 and 345 allow servicing of the check valve 365. The ball valves 345 and 350 enable the clean liquid flow meter 380 to be serviced. In some embodiments, the 390 connection of clean water effluent may be connected to a holding tank, storm drain or other method to control clean water pumped out of the system. In some embodiments, clean water can be recycled to one or more components of the water decontamination system. In one embodiment, the clean water can be transported back to the separation tower 200 for further processing. In another embodiment, the clean water can be processed by one or more separation towers, which are similar to or different from the separation tower 200. In some embodiments, the clean water can be recycled to the aeration module 10 or different aeration modules. In addition, clean water can be processed by one or more other treatment methods, such as passing clean water through an activated carbon filter. The person having ordinary skill in the art will understand many ways to further process water contaminated by one or more of the components of the water decontamination system, described herein or other decontamination processes, such as water treatment processes. municipal.

Contaminated gas phase treatment systems In some embodiments, the contaminated gas phase is transferred to a contaminated gas phase treatment system 201. In one embodiment, the liquid decontamination system comprises one or more contaminated gas treatment systems 201, 202. The one or more systems of Contaminated gas treatment can reduce the levels of pollutants in the contaminated gas. In one embodiment, the contaminated gas phase is transferred from the aeration module 10 to the contaminated gas phase treatment system 201. In another embodiment, the contaminated gas phase is transferred from the separator tower 200 to the contaminated gas phase treatment system 201. In some embodiments, the contaminated gas phases of the separator tower 200 and the aerator module 10 are transferred to the contaminated gas phase treatment system 201. This transfer can occur at the same time, which causes the contaminated gas phases of the aerator module 10 and the separator tower 200 to be mixed before the treatment. However, these phases of contaminated gas can be treated separately by one or more treatment systems. In certain embodiments, the contaminated gas phase is treated in such a manner that a gas phase comprising substantially no contaminants can be released into the environment. Contaminants in the contaminated gas phase can be trapped or transformed into other compounds that are safe to release into the environment. In one embodiment, the treated gas phase can be reused in one or more components of the liquid decontamination system. In one embodiment, the contaminated gas phase treatment system 201 is configured to remove or change Gas phase pollutants from other gases that can be expelled from the system as exhaust. In some embodiments, the gas phase pollutants are oxidized. In one embodiment, contaminated gas phase pollutants are converted to carbon dioxide and water. Then oxidized contaminants can be released into the atmosphere. In another embodiment, the gas phase pollutants are condensed. Other process gases, such as remaining dilution air, as well as other environmentally safe compounds, can be released into the atmosphere. In another embodiment, the gas phase pollutants are adsorbed. The remaining dilution air and non-adsorbed gases can be released into the atmosphere. In addition, the contaminated gas phase may be subjected to one or more treatment systems to remove contaminants from the gas phase. The one plus 201 gas phase treatment systems 201 may vary according to the contaminants. Suitable contaminated gas phase treatment systems include but are not limited to one or more of electrical catalytic oxidant (see Figure 12), thermal oxidizers, adsorption filtration systems (see Figure 13), which include filtration systems by adsorption of carbon, zeolite and filtration systems by polymeric adsorption, condensers (see Figure 14), oxidants to the flame, cryogenic treatment processes, gas cooling and liquefaction, regenerative thermal oxidants and rotating concentrators. Some of these treatment systems are described further herein. Some gas phase treatment systems 201 may be limited in the amount or proportion of gaseous pollutants they receive and / or treat. In addition, the amount of exhaust that can be released is often determined by environmental regulations governing the compounds in the exhaust. Similarly, such contaminated gas phase treatment systems 201 may also be limited in the release of byproducts from such treatment processes to the atmosphere. To regulate the amount and concentration of pollutants subjected to treatment in system 201 of the contaminated gas phase treatment, the flow rates of the contaminated gas phase can be controlled. For example, the amount of dilution received with the contaminants can be controlled. As described above, the dilution air can be mixed with the contaminated gas phase in the separator tower module 200. However, the dilution air can also be mixed with the contaminated gas phase outside the separator tower 300. In some embodiments, the treatment system 201 may require additional dilution air to process the phase of contaminated gas In such instances, the treatment system 201 may point to the dilution air valve 415 that allows an increase in dilution air to enter the contaminated gas phase. Such signaling can occur manually or automatically based on a programmable logic control in the control panel. In some embodiments, the contaminated gas treatment system 201 can detect a quantity or concentration of contaminant that exceeds that allowed by regulation. Such excess levels may require additional dilution or stoppage of the liquid decontamination system. In one embodiment, one or more components of the liquid decontamination system may discontinue additional processing of one or more of the contaminated gas, contaminated liquid, contaminated gas, air dilution or decontaminated liquid. In some embodiments, the cessation of one or more of the components mentioned above may allow the processing system to reduce contaminant levels. When the system detects that one or more of the contaminants has reached a designated level or safe level or a level prescribed by environmental laws, then the system may optionally initiate one or more components of the liquid decontamination system. Several examples of certain equipment systems are described later in this: Electric Catalytic Oxidizer Some liquid decontamination systems as described herein comprise a catalytic oxidant module. In some embodiments, the catalytic oxidant is an electrical catalytic oxidant 100. In some embodiments, the catalytic oxidant module 100 can receive a contaminated gas phase from the separation tower 200. In some embodiments, the catalytic oxidant module receives a phase of contaminated gas from the aerator module 10. In certain embodiments, the catalytic oxidant module 100 receives more than one contaminated gas phase, in which the contaminated gas phases of the aerator module 10 and the separator tower 200 are included. This process It can remove up to 99.99 percent of the target contaminants and produce exhaust that can be released into the environment. Modes of catalytic oxidants may vary. Referring to Figure 12, some embodiments of catalytic oxidants will include a catalyst 570. Other embodiments include a heater 570 that heats the contaminated gas phase prior to introduction to the catalyst 570. Figure 12 depicts a non-limiting example of a catalytic oxidant module. 100 electric. The electrical catalytic oxidant 100 is equipped with an oxidant fan 520, flame arrester 530, pitot tube 540, air-to-air heat exchanger 550, electric heater 560, catalyst 570 and Exhaust chimney 580. The electric catalytic oxidant 100 is also equipped with pressure switches, temperature switches and temperature detectors to control the process of oxidizing the process gas. The process gas passes through a pipe 511 to the electrical catalytic oxidant 100. The process gas enters the electrical catalytic oxidant 100 through the null bell 590 in the oxidant fan 520. The null bell 590 can balance the amount of phase of contaminated gas and dilution air entering the electrical catalytic oxidant 100. In some embodiments, the null bell 590 in conjunction with the oxidant fan 520 balances the dilution air and process gas to ensure that the temperature of the process gas / Dilution air is at the correct temperature as it approaches and as it is treated by the catalyst. Thus, these components can prevent a high temperature alarm 605 in the electrical catalytic oxidant 100 from being activated. In some embodiments, the oxidant fan blows the process gas and an additional dilution air at a flow rate of 200 SCFM, in which approximately 50, 100 and 150 SCFM are included. Referring to Fig. 12, the flame arrester 530 prevents flame propagation back to the process gas source. Several other instruments are designed to control the electrical catalytic oxidant 100. These instruments include an averaging pitot tube 540, a flow indicator 610, a differential pressure transmitter 615, a pressure indicator 620, a pressure switch 625, a pressure alarm 630 and a sample gate 635. The tube 540 averaging pitot measures the total flow velocity of process gas. The differential pressure transmitter 615 converts the pressure signal from the averaging pitot tube 615 to a milliamp signal. The milliampere signal can be used to determine the flow velocity of the process gas. The signal can be fed to the control panel. In addition, the signal can be displayed on a chart recorder. The chart recorder shows the flow rate in standard cubic feet per minute and also records the flow rate. Referring to Figure 12, the pressure switch 625 monitors the pressure of the process gas entering the oxidizing chamber. If the pressure is not above a pre-set minimum pressure, the pressure switch 625 is deactivated and sends a signal to the programmable logic controller in the control panel. Then the programmable logic controller paralyzes at least part of the process. The gauge 620 indicates the gas pressure of the process entering the oxidizing chamber. Some embodiments may also include a heat exchanger 550. The air-to-air heat exchanger 550 is adapted to preheat the process gas that enter the oxidizing chamber. The air-to-air heat exchanger 550 utilizes the hot process gas leaving the catalyst 570 to heat the cold process gas entering the air-to-air heat exchanger tube site 550. As discussed above, the heater Electric 580 is designed to increase the process temperature, which includes the contaminated gas phase. Downstream of electric heater 580 are catalyst 570 and differential pressure switch 650 of the catalyst. The differential pressure switch 650 monitors the pressure drop through the catalyst 570. If the pressure drop increases to a pre-set differential pressure, the switch is activated and sends a signal to the programmable logic controller. Then the programmable logic controller paralyzes at least part of the equipment. The thermocouple 680 is located on the upstream side of the catalyst 560 and measures the temperature of the process gas entering the catalyst 570. If the temperature in the thermocouple 680 is too low, the electric heater 560 is energized by the control panel. If the temperature in the thermocouple 680 is too high, the electric heater 560 is de-energized by the control panel. If the temperature in the thermocouple 680 reaches a pre-set high temperature, a signal is sent to the programmable logic controller. Then he programmable logic controller turns off the computer. The thermocouple 670 is located on the downstream side of the catalyst 570. The thermocouple 670 monitors the temperature of the process gas leaving the catalyst 570. If the temperature in the thermocouple 670 reaches a pre-set temperature, a signal is sent to the logic controller programmable. The programmable logic controller sends a signal to the oxidant fan 520 to be accelerated. As the fan 520 is accelerated, more dilution air is driven into the oxidizing gas chamber, which cools the temperature in the thermocouple 670. If the temperature in the thermocouple 670 rises to a pre-set temperature, a signal is sent to the programmable logic controller. Then the programmable logic controller shuts down the equipment. The gas that has been processed by the catalyst can leave the catalytic oxidant 100 in the exhaust stack 580. In some embodiments, the exhaust stack 580 is equipped with a sampling port 680, which is used to collect gas samples effluent. In some embodiments, the 580 exhaust chimney vents the hot process gas to the atmosphere. In other embodiments, the 580 exhaust stack recycles the processed gas to the water decontamination system. Each catalytic oxidant can have different conditions that produce the best result. These conditions they are likely to depend on variables such as the type of catalyst, the flow velocity, temperature, particular pollutants and the concentration of the contaminated gas. A non-limiting example of the electrical catalytic oxidant that can be used is CCC SRCO 250E, available from Catalytic Combustion (Drewelow Remediation Equipment, Inc.). In this example, the contaminated gas phase passing through the catalytic bed is at a temperature of about 343 ° C (650 ° F).

Condenser System A method of treating a contaminated gas phase includes condensing the contaminants in the gas phase. In some embodiments, the water decontamination system includes a condenser system. As discussed above, the condenser system may comprise a condenser that is either cooled by air or cooled by water. In some embodiments, the condenser system comprises a condenser that is cooled by contaminated water. In these modalities, the heat generated from the condensation of the contaminated gas phase can be exchanged with the contaminated water. In some embodiments, the condenser system is adapted to condense one or more of 1,1,1-trichloroethane, 7 1, 1, 2, 2-tetrachloroethane, 1, 1, 2-trichloroethane, 1,1,2-trichlorotrifluoroethane, 1,1-dichloroethane, 1,1-dichloroethene, 1,2,3-trimethylbenzene, 1, 2, 4-trichlorobenzene, 1,2,4-trimethylbenzene, 1,2-dibromoethane, 1,2-dichlorobenzene, 1,2-dichloroethane, 1,2-dichloropropane, 1,2-dichlorotetrafluoroethane, 1, 3, 5-trimethylbenzene, 1,3-dichlorobenzene, 1,4-dichlorobenzene, 2, 3-dimethylpentane, 2,4-dimethylpentane, acetone, alpha-pinene, benzene, bromomethane, carbon tetrachloride, chlorobenzene, chloroethane, chloroform, chloromethane, cis-1,2-dichloroethene, cis-1,3-dichloropropene, cycloheptane, cyclohexane, dichloro-difluoromethane, d-limonene, ethyl alcohol, ethylbenzene, ethylcyclohexane, ethyl methacrylate, hexachloro-1,3-butadiene, iso-octane, isoprene, isopropylbenzene, m, p-xylene, methylethyl ketone, methyl isobutyl ketone, methylcyclohexane , methylene chloride, methylmethacrylate, methyl-tert-butyl ether, n-butylbenzene, n-decane, n-dodecane, n-heptane, n-hexane, n-nonane, n-octane, n-propylbenzene, n-undecane, or -xylene, sec-butylbenzene, styrene, tert-butylbenzene, tetrachloroethene, tetrahydrofuran, toluene, trans-1,3-dichloropropene, trichloroethene 400 trichlorofluoromethane, vinyl chloride and other volatile organic compounds. Referring to Figure 13, the condenser system 800 may be equipped with one or more of a contaminated gas tributary connection 805, condenser 810, contaminated liquid effluent connection 815, connection 820 Clean air effluent and clean air flow meter 825. Process gas enters condenser system 800 at tributary connection 805. As the contaminated gas phase passes through condenser 810, at least some contaminants they condense to concentrated liquid pollutants. The liquid contaminants can be removed from the condenser 810 in the effluent connection 815. The ball valve 830 can be left open to continuously allow the condensed contaminants to be removed from the condenser system 800. Alternatively, the ball valve 830 can be closed to allow contaminants to be collected in the condenser 810. In some embodiments, clean air can be vented from the condenser 810. This clean air can leave the condenser at connection 820 of the clean air effluent and be captured or vented to the atmosphere . The clean air. it can alternatively be recycled into one or more components of the liquid decontamination system. Such a clean air outlet can be monitored by the 825 clean air flow meter. A non-limiting example of a capacitor system is described above. The person having ordinary skill in the art will recognize the interchangeability of various elements of different modalities with the described condenser system and other condenser systems available. A liquid decontamination system that includes at least one aerator module 10, at least one separator tower 200 and at least one condenser system 800 may be particularly suitable for applications that recover fuel and other volatile water contaminants. Such fuel or other contaminants can then be recycled to various processes in which it was produced. For example, ships and other marine vehicles frequently collect bilge water. The bilge is the compartment at the bottom of the hull of a ship or other marine vessel, where the water is collected, so that it can be pumped out of the ship at a later time. Bilge water often includes fuel and other volatile organic pollutants. By using a liquid decontamination system, which includes a condenser system, fuel and other volatile organic pollutants can be recovered. Such fuel and other contaminants could then be recycled as fuel for the ship or marine vessel.

Adsorption filter As discussed above, water decontamination systems as described herein, may include an adsorption filter 700 that treats the phase of contaminated gas Suitable adsorption filter systems include, but are not limited to, activated carbon filtration systems, zeolite filtration systems, and polymer filtration systems. Referring to Figure 14, in some embodiments, the adsorption system 700 may receive a contaminated gas phase from the separation tower 200. In some embodiments, the vacuum pump 510 feeds the contaminated gas phase to the adsorption system 700. In some embodiments, the adsorption system 700 receives a contaminated gas phase from the aerator module 10. In certain embodiments, the adsorption filtration system 700 receives more than one phase of contaminated gas, which includes the phases of contaminated gas from the module. aerator 10 and separation tower 200. In one embodiment, the adsorption filtration system 700 comprises an activated carbon filter that is suitable for removing contaminants from liquids. In some embodiments, the activated carbon filtration system is particularly appropriate for removing certain contaminants from the water. In some embodiments, the adsorption filtration system comprises one or more absorption vessels 705, 710. In particular embodiments, these adsorption vessels 705, 710 are containers of activated carbon. Such carbon containers can be carbon containers in gaseous phase as the gaseous pollutants are purified in the container. In some embodiments, the gas phase contaminants may be first condensed and then purified through such adsorption vessels 705, 710. The adsorption vessels may be selected based on the contaminant to be purified from the liquid and gaseous phase. Additionally, the containers can be selected based on the desired flow rates of the overall process. In one example, an activated carbon container can be selected based on at least one contaminant, such as aromatic hydrocarbons or halogenated organic compounds to be removed. In some embodiments, the activated carbon filtration system is adapted to adsorb vinyl chlorides, 1,2-dichloroethane, carbon tetrachloride, trichlorethylene, tetrachlorethylene, 1,1-dichloroethane, chloroform, 1,1,1-trichloroethane, 1 , 1,2-trichloroethane and combinations thereof. In other embodiments, the activated carbon filtration system is adapted to adsorb certain VOCs. In some embodiments, the adsorption system can remove volatile organic compounds from the contaminated gas stream as the contaminated gas is passed over the adsorption filter. A method of treating a contaminated gas phase, either from the separation tower 200 or The aerator module 10 includes adsorbing the contaminants by adsorption by activated carbon. In some embodiments, the liquid purification system comprises an activated carbon filtration system. The activated carbon filtration system may comprise one or more vapor phase carbon containers, including, but not limited to, two, three, four and five carbon containers. The contaminated gas phases are passed through the vapor phase carbon containers. Referring to Figure 14, the adsorption filtration system 700 can include two purification vessels 705, 710, three sampling gates 715, 720, 725, three manual ball valves 730, 735, 740 and an exhaust stack . The process gas passes through a pipe 741 to the adsorption filtration system 700. The process gas can enter the adsorption filtration system 700 through the process gas tributary connection 745. The averaging Pitot 750 measures the total flow rate of the process gas that is treated by the adsorption filtration system 700. The temperature gauge 755 measures the temperature of the process gas being treated. The pressure gauge 760 measures the pressure of the process gas that is treated. The sample gate 715 is used to collect a sample of process gas before treatment. The adsorption vessels 705, 710 can be used to treat the process gas. Such process gas enters the adsorption vessels 705, 710 through the tributary connections 765,775. In the described embodiment, the tributary connections 765, 775 are located near the bottom of the adsorption vessels 705, 710. The process gas flows upwardly through the adsorption means 706, 711, such as activated carbon, and the Adsorption medium adsorbs the contaminants in the process gas. The process gas leaves the adsorption vessel 705, 710 at the effluent connections 770, 780. In this embodiment, the effluent connections 770, 780 are located near the top of the adsorption vessels 705, 710. The gate Sampling 720 is used to collect a sample of process gas after treatment by the primary adsorption vessel 705. The ball valves 730 and 735 allow serving the primary adsorption vessel 705. Optionally, the secondary adsorption vessel 710 can be used to further purify the contaminated gas phase leaving the adsorption filter 705. The ball valves 735 and 740 allow the secondary carbon vessel 710 to be serviced. Downstream of the effluent connection 780 is the chimney 751. Exhaust chimney 751 may be equipped with a sampling port 725. Then the purified gas phase may exit from the 751 exhaust fireplace to the environment or be recycled to the water decontamination system. Examples of appropriate activated carbon filters and containers suitable for use in the liquid purification system include, but are not limited to, MX-200-V available from Barnebey Sutcliffe, AP3-60 and AP4-60 available from the Calgon Carbon Corporation . In some embodiments, activated charcoal can be activated charcoal. In some embodiments, the activated carbon has a minimum hardness number ranging from about 60 to about 120, and more preferably about 90. The density of activated carbon can range from about 300 to about 600. In other embodiments, the density of the activated carbon activated carbon can range from about 400 to about 500, and more preferably about 450 to about 500. In most cases, the activated carbon has a moisture content that is not more than 5% by weight.

Double phase Water decontamination systems as described herein can also be used in a double phase capacity. Frequently, a contaminated source of groundwater will also include gaseous pollutants. Such contaminants can also be processed by liquid decontamination systems and be removed by the contaminated gas treatment system. In one embodiment, the gaseous pollutants are extracted from the soil or soil and enter the aerator module. Such contaminants can pass directly into the upper space of the aerator tank and be transferred to the contaminated gas treatment system. However, some embodiments may include a detector that can recognize gaseous pollutants that are extracted from the ground or soil. Such a detector can then put into operation a valve that allows the gaseous pollutants to pass directly to the contaminated gas treatment system.

Assembly configuration The liquid decontamination system can be mounted on one or more platforms. In one embodiment, each module of the water decontamination system is mounted on a separate spar. In such modality, the user could choose the components and assign each component to the desired site. However, in some embodiments, it is advantageous to mount all the modules on a platform. An example of a configuration is shown in Figures 15 and 16. In these figures, the aerator tank 101 is mounted on a first stringer 67. The filtration module 300, the separator tower 200 and the contaminated gas treatment system 201 they are mounted on a second stringer 68. Additionally, the second stringer includes the water transfer pump 90, vacuum pump 510, compressor 20. As indicated in the Figures, the separator tower module may include two spacer towers 200 and 203. Alternatively, the Separating tower 203 can be mounted on spacer tower 200. As shown, spacer tower 203 can be removed for ease of transportation of spar 68.

Manual or automatic control As stated in the entire description, one or more processes and / or components can be controlled manually or automatically. Several valves, pressure gauges, temperature gauges and pump controls allow the user to manually determine the operating conditions of the water decontamination system. In some modalities, it is preferable that these processes be controlled automatically. For example, one or more of the processes can be controlled from a control panel. In some embodiments, the control panel comprises one or more programmable logic controllers. Each controller can be designed for certain processes to monitor, adjust, activate or deactivate, depending on the pre-programmed settings and conditions. The ways to control these processes automatically, will be understood by the person having ordinary skill in the art.

Unless otherwise indicated, the term "logical processing controller" is a broad term and is used in its ordinary sense and includes, without limitation, when the context permits, one or more stages, one or more groups , one or more programs, one or more instructions and one or more processors. It can also refer to the logic implemented in physical elements or fixed elements, or to a set of instructions for programming elements, which possibly has entry and exit points, written in a programming language, such as for example C or C ++. A processing module can be compiled and linked to an executable program, installed in a dynamic link library, or it can be written in an interpreted programming language, such as for example BASIC, Perl or Python. It will be appreciated that the processing modules may be callable from other modules (such as an input module) or from themselves, and / or may be invoked in response to events or interruptions detected. It will be further appreciated that the processing modules may consist of connected logic units, such as gates and joggers, and / or may consist of programmable units, such as programmable gate arrays or processors.

EXAMPLES AND TESTS Referring to Figure 17, a system of Liquid decontamination was built and tested. This system included an aerator module 10, a liquid transfer pump 90, filtration system 300, separator tower 200, vacuum pump 510, an electrical catalytic oxidant 100. Additionally, a heat exchanger 58 was installed to transfer heat from the liquid transfer pump 90 to the contaminated water before it enters the separator tower 200. All of these components are described herein. Samples of contaminated water were tested. These samples contained several contaminants, such as VOC. Then the samples were purified using the liquid decontamination system, the samples were introduced at the affluent liquid connection point in the aerator module 10. Between samples, unpolluted water was run through the liquid decontamination system by several hours . The operating conditions of the water decontamination system were varied to determine the appropriate conditions for purifying the various contaminants in the water. One or more of the water flow rate, water pressure, water temperature, nozzle pressure, vacuum pressure of the separator tower, separator tower temperature, and dilution air flow rate can be varied to adjust certain contaminants and conditions of field In some embodiments, the liquid purification system as described herein operates to produce approximately 37.8 liters (10 gallons) per minute of purified liquid. However, the liquid purification system can be configured and / or scaled to produce more or less than 37.8 liters (10 gallons) per minute, depending on the application and / or contaminants. The samples were tested under the operating conditions described in Table 1.

The samples that were introduced to the liquid decontamination system were tested to determine the initial concentration of the contaminants in the sample. This is referred to as the "affluent" concentration in the following tables. After the introduction of the sample to liquid decontamination system, additional aliquots were taken at different points to determine the effectiveness of the various components of the liquid decontamination system. Aliquots of "midpoint" were taken immediately after the aeration tank to determine the efficiency of the aerator module 10. Aliquots of "effluent" were taken after the water was removed from the sump of the separating tower. In addition, samples 4 and 6 present data describing the change in the effectiveness of contaminants based on the dilution air flow rate. Note that some of the data presented in the tables are given in terms of "<" (less than) of some value due to the detection limits of the GC-MS testing device. The following Tables 2-7 detail the results of the tests: Table 2 Table 3 Table 4 Sample 3 Point Affluent medium Effluent Compound (μ? / 1) (μ? / 1) (μß / 1) Benzene 1580 26 5.8 Ethyl Benzene 2940 367 81 Toluene 15700 832 147 Total Xylenes 15700 2330 563 MTBE 14800 919 320 Gasoline 90400 9590 4000 Table 5 Table 6 Sample 5 Point Mean effluent Compound (ug / 1) (R / l) (μ? / 1) Benzene 8700 < 50 < 10 Ethylbenzene 14100 221 43 MTBE 158000 1100 248 Toluene 50600 414 235 Total xylenes 48900 1100 238 Gasoline 292000 11200 4160 Table 7 According to the data, the liquid decontamination system substantially reduces the amount of contaminants in contaminated water samples. Specific contaminants can be removed in larger quantities by varying the conditions of the liquid decontamination system. In addition, in all samples, a clean exhaust was released to the environment in accordance with environmental regulations. Other examples of water decontamination systems are described herein. Still another example is the water decontamination system of Figure 18. In this embodiment, contaminated water passes through a first filtration system 909. This prevents solid particles from entering the aerator module 10 or any other component of the system. decontamination of water. Then the contaminated water enters the aeration module 10 and is decontaminated according to the processes described above. Since water can not being at the selected temperature for decontamination, water can pass through the aeration module 10. In some embodiments, the system does not purify water that is not at the selected temperature. In other embodiments, the water is decontaminated in the aerator module at temperatures lower than the selected temperature. As the water is transferred from the aeration module 10 by the liquid transfer pump 90, water can be directed to the filtration system 300. Alternatively, if the water is not at a selected temperature, the water can be transferred and / or processed by the 911 heat exchanger. This can be carried out manually or automatically. For example, this can be carried out by the solenoid 913 which can automatically direct the water to the heat exchanger 911. The heat exchanger 911 exchanges the heat of the vacuum pump with the contaminated water. In some embodiments, the contaminated water can then be transferred back to one or more components of the water decontamination system for further purification. For example, after passing through the heat exchanger 911, the heated contaminated water can pass back through the filtration system 300 or back to the aerator module 10. In another embodiment, the contaminated water can pass through the 921 heat exchanger catalytic oxidant electrical 100 or more in general, a heat exchanger 921 of the contaminated gas treatment system 201. In one embodiment and as illustrated in Figure 14, contaminated water may pass through the 911 heat exchanger and the heat exchanger 921, before going back to one or more components of the liquid decontamination system, such as the aerator module 10, the filtration system 300 or the separator tower 200. By allowing the water to pass through both the exchangers of heat, the water is heated more efficiently during the decontamination process. After sufficient heating, the solenoid valve 913, 914 can redirect the water to the aerator module or the filtration module. As the water leaves the aeration module at or above the selected temperature range, the water can then flow through the filtration system 300 and the separating tower 200. The contaminated water can then be further purified by removing the pollutants to a contaminated gas phase. Then this phase of contaminated gas can be purified through a contaminated gas phase treatment system such as the electrical catalytic oxidant 100. The various methods and techniques described above provide a variety of ways to carry out the invention. Of course, it will be understood that not necessarily all the objects or advantages described can be obtained in accordance with any particular modality described herein. In addition, the one experienced in the art will recognize the interchangeability of various elements of different modalities. Similarly, the various elements and steps discussed above, as well as other known equivalents for each of such elements or steps, can be mixed and matched by one of ordinary skill in the art to effect the methods in accordance with the principles described in I presented. Although the invention has been disclosed in the context of certain embodiments and examples, it will be understood by those skilled in the art that the invention extends beyond the modalities disclosed specifically to other alternative embodiments and / or uses and modifications and obvious equivalents of the same. Thus, the invention is not intended to be limited by the specific disclosures of preferred embodiments herein.

Claims

CLAIMS 1. A system characterized in that it comprises: an aerator module configured to convert one or more pollutants in a contaminated liquid to gaseous phase contaminants; a separating tower configured to convert the contaminated liquid to a contaminated gas phase and a liquid with reduced levels of one or more pollutants; and a contaminated gas treatment system configured to receive the contaminated gas phase and the gas phase contaminants; where the contaminated gas treatment system reduces the levels of contaminants in the contaminated gas phase and the gas phase pollutants. The system according to claim 1, characterized in that the aerator module comprises a plurality of nozzles, wherein the nozzles are configured to feed gas bubbles to the contaminated liquid. 3. The system according to claim 1 or 2, characterized in that the aerator module operates under a static or dynamic vacuum. 4. The system according to any of claims 1, 2 or 3, characterized in that the separating tower comprises a high vacuum environment. 5. The system according to any of claims 1, 2, 3 or 4, characterized in that the separating tower comprises a plurality of nozzles that receive the contaminated liquid and are configured to convert the contaminated liquid to an atomized contaminated mist. The system according to claim 5, characterized in that the contaminated mist is converted to the contaminated gas phase and the liquid with reduced levels of the one or more pollutants. The system according to any of claims 1 to 6, characterized in that the liquid with reduced levels of the one or more pollutants comprises less than about 5% of the contaminants in the contaminated liquid. The system according to claim 7, characterized in that the liquid with reduced levels of one or more contaminants comprises less than about 1% of the contaminants in the contaminated liquid. The system according to claim 8, characterized in that the liquid with reduced levels of one or more contaminants comprises less than about 0.5% of the contaminants in the contaminated liquid. The system according to claim 9, characterized in that the liquid with reduced levels of one or more contaminants comprises less than about 0.1% of the pollutants in the contaminated liquid. The system according to any of claims 1 to 10, characterized in that the one or more contaminants are volatile organic compounds. The system according to any of claims 1 to 11, characterized in that the contaminated gas treatment system reduces the levels of contaminants by one or more processes selected from the group consisting of adsorption, oxidation and condensation of the contaminants. The system according to any of claims 1 to 12, characterized in that the aerator module, the separator tower and the contaminated gas treatment system are in communication with a controller. 14. The system in accordance with the claim 13, characterized in that the controller is capable of activating or deactivating one or more of the aerator module, the separator tower, the contaminated gas treatment system. The system according to any of claims 13 or 14, characterized in that the controller is able to regulate one or more of the aerator module, the separating tower and the contaminated gas treatment system. 16. The system according to any of claims 13, 14 or 15, characterized in that the controller is able to regulate the transfer of tributary or Effluent of water to or from one or more of the aerator module or the separator tower. 17. The system according to claim 13, 14, 15 or 16, characterized in that the controller is able to regulate the flow of contaminated gas from one or more of the aerator module and separator tower. 18. The system according to any of claims 1 to 17, characterized in that the system is configured to extract and treat a contaminated gas from the soil, where the contaminated gas does not comprise a contaminated liquid. 19. A system characterized in that it comprises: An aerator module configured to convert one or more contaminants in a contaminated liquid into gaseous phase contaminants; a contaminated gas treatment system configured to receive the gas phase pollutants; where the contaminated gas treatment system reduces the levels of contaminants in the gas phase pollutants. 20. A system characterized in that it comprises: a separating tower configured to convert a contaminated liquid to a contaminated gas phase and a liquid with reduced levels of one or more contaminants; and a contaminated gas treatment system configured to receive the contaminated gas phase; where the contaminated gas treatment system reduces the levels of contaminants in the contaminated gas phase. 21. The system according to claim 19 or 20, characterized in that the liquid with reduced levels of the one or more contaminants is substantially free of contaminants. 22. The system according to claim 20, characterized in that the separating tower receives a dilution zone. 23. The system according to claim 22, characterized in that the dilution air is mixed with the contaminated gas phase in the separator tower. 24. The system according to claim 22 or 23, characterized in that the contaminated gas phase treatment system is configured to control the amount of the dilution air. 25. The system according to any of claims 1 to 24, characterized in that the contaminated liquid is contaminated water. 26. A method for reducing the levels of contaminants in a contaminated liquid, characterized in that it comprises: aerating the contaminated liquid to produce a first contaminated gas phase; converting the contaminated liquid to a contaminated mist in a separating tower; converting the contaminated mist to a second phase of contaminated gas and a liquid mist by subjecting the contaminated mist to a high vacuum environment within the separation tower; and treating the first and second phases of contaminated gas in a treatment system. 27. The method of compliance with the claim 26, characterized in that the treatment step comprises the recovery of the pollutants from the first and second phases of contaminated gas. The method according to claim 26 or 27, characterized in that the treatment step comprises oxidizing or reducing the contaminants of the first and second phases of contaminated gas. 29. The method according to claim 26, 27 or 28, characterized in that it further comprises transporting the second contaminated gas phase outside the separating tower by vacuum. 30. The method according to any of claims 26 to 29, characterized in that it further comprises transporting the second phase of contaminated gas away from the separating tower using a dilution air. 31. The method according to any of claims 26 to 30, characterized in that it further comprises combining the first and second gas phases contaminated before treatment by the treatment system. 32. The method according to any of claims 26 to 31, characterized in that it further comprises regulating one or more stages with a controller. 33. The method according to any of claims 26 to 32, characterized in that it also comprises collecting clean water from the separating tower. 34. A method for receiving the levels of contaminants in a contaminated liquid, characterized in that it comprises: converting the contaminated liquid to a contaminated mist in a separating tower; converting contaminated fog to contaminated gas and liquid mist by subjecting the contaminated mist to a high vacuum environment within the separation tower; reduce the levels of pollutants in the contaminated gas through a contaminated gas phase treatment system. 35. The method according to claim 34, characterized in that the contaminated gas treatment system comprises an electrical catalytic oxidant. 36. The method according to the claims 34 or 35, characterized in that the step of converting the contaminated liquid to a contaminated mist comprises: providing the contaminated liquid to an air separator; reduce the pressure of the air separator with a vacuum source; atomizing the contaminated liquid to a contaminated mist through a plurality of nozzles near the top of the air separator; allow the mist to fall gravitationally inside the air separator, to make air flow in a direction countercurrent to the gravitational drop of the mist. 37. The method according to the claim 36, characterized in that it further comprises controlling the air flow rate in the air separator with a controller. 38. The method of compliance with the claim 37, characterized in that the controller is capable of activating or deactivating the vacuum source, the air flow or a contaminated gas treatment system in fluid communication with the vacuum source. 39. A method for receiving the levels of contaminants in a contaminated liquid, characterized in that it comprises: aerating the contaminated liquid in an aeration module to produce a first phase of contaminated gas; transporting the first phase of contaminated gas to one or more treatment systems; and reduce the levels of contaminants in the contaminated gas phase in the one or more treatment systems. 40. The method of compliance with the claim 39, characterized in that it further comprises collecting the contaminated liquid after aeration, wherein one or more of the contaminants of the contaminated liquid is MTBE, and wherein the aeration step removes at least about 98 percent of the MTBE from the contaminated liquid. 41. The method according to the claim 40, characterized in that it further comprises collecting the contaminated liquid after aeration, wherein one or more of the contaminants of the contaminated liquid is MTBE, and wherein the aeration step removes at least about 99 percent of the MTBE from the contaminated liquid. 42. The method according to any of claims 26 to 41, characterized in that it also comprises filtering the contaminated liquid. 43. The method according to any of claims 39 to 42, characterized in that it further comprises: receiving a second phase of contaminated gas in the aeration module of a contaminated gas source; transporting the second phase of contaminated gas in the aeration module to one or more treatment systems; and reduce pollutants in the second phase of gas contaminated with the one or more treatment systems. 44. The method according to claim 43, characterized in that it further comprises mixing the second phase of contaminated gas with the first phase of contaminated gas. 45. The method according to claim 43, characterized in that the contaminated gas source is the soil. 46. An apparatus for reducing the levels of one or more contaminants in contaminated water, the apparatus is characterized in that it comprises: a first container configured to receive contaminated water; the container comprises: one or more side walls, one or more lower walls; and one or more upper walls, the one or more side walls, the one or more lower walls and the one or more upper walls are in contact to define the interior of the container; a first entry in fluid connection with a source of contaminated water; at least a second entry in fluid connection with a gas source; a first outlet in fluid connection with a liquid transfer pump - a second outlet coupled to a first vacuum source; wherein the interior is adapted to contain contaminated liquid and the second inlet is configured to feed a gas to the contaminated liquid; a tower in fluid connection with the liquid transfer pump, the tower comprises: a third inlet for receiving the contaminated liquid from the liquid transfer pump; a vacuum chamber, the vacuum chamber has a third outlet coupled to a second vacuum source; and a plurality of nozzles in fluid connection with the third inlet, the plurality of nozzles are configured to feed the contaminated liquid into the vacuum chamber as an atomized liquid; a bottom to receive a clean contaminated liquid, and a fourth outlet located near the bottom to remove the clean contaminated liquid. 47. The apparatus according to claim 46, characterized in that the at least one second inlet is connected to a gas manifold located at least partially within the interior of the container, the gas manifold comprises a plurality of orifices configured to feed air to the contaminated water in the first container. 48. The apparatus according to claim 46 or 47, characterized in that the source of contaminated water is one or more means for water treatment. 49. The apparatus according to claim 46, characterized in that the contaminated water source is the soil. 50. The apparatus according to any of claims 46 to 49, characterized in that the first container is a container with baffles. 51. The apparatus according to any of claims 46 to 50, characterized in that the first container comprises a plurality of surfaces adapted to create an indirect path for contaminated water within the interior of the container. 52. The apparatus according to any of claims 46 to 51, characterized in that at least some of the orifices of the gas manifold are located near one or more walls of the bottom of the container. 53. The apparatus according to any of claims 46 to 52, characterized in that the interior of the container comprises two or more chambers, each chamber partially separated by a set of walls, wherein at least Some of the walls define holes between each chamber to allow contaminated water to pass through the two or more chambers. 54. The apparatus according to claim 53, characterized in that a gas manifold has one or more holes for creating bubbles within one or more of the chambers, the gas manifold is fluidly connected to the second inlet. 55. The apparatus according to any of claims 46 to 54, characterized in that it further comprises: means for the treatment of a contaminated gas, the treatment means fluid connection with the third outlet of the vacuum chamber. 56. The apparatus according to any of claims 46 to 55, characterized in that it further comprises a contaminated gas treatment system in fluid connection with the second outlet of the first container and the third outlet of the vacuum chamber. 57. The apparatus in accordance with the claim 56, characterized in that the contaminated gas treatment system is one or more selected from the group consisting of an electrical catalytic oxidant, a thermal oxidant, an adsorption filtration system, a condenser, an oxidant to the flame, a treatment system cryogenic, a gas cooling and liquefaction system, regenerative thermal oxidizers and rotating concentrators. 58. An apparatus characterized in that it comprises: a tank for containing a liquid, the tank comprises a first inlet for the transport of affluent of the liquid, a first outlet for the transport of the liquid effluent and a second outlet for the transport of effluent from a contaminated gas, the tank further comprises a plurality of baffles, each baffle being mounted within the tank in substantially parallel positions, wherein the liquid of the first inlet is configured to travel in one or more chambers within the tank at the first outlet, each chamber is separated by at least one of the plurality of baffles and each chamber comprises a gas supply system for bubbling a gas through the liquid - a first source of vacuum in fluid connection with the second outlet of the tank, the source of vacuum it is configured to feed the contaminated gas to a gas treatment system. 59. The apparatus in accordance with the claim 58, characterized in that it also comprises a gas treatment system. 60. The apparatus according to claim 0 or 59, characterized in that the first source of vacuum is at least a portion of a system of gas treatment. 61. The apparatus according to any of claims 59 or 60, characterized in that the gas treatment system is an electrical catalytic oxidant and the at least one portion is an oxidant blower capable of creating the vacuum source. 62. The apparatus according to any of claims 58 to 61, characterized in that it further comprises an air separator in fluid connection with the first outlet, the air separator in the form of a cylindrical column, the column comprises a plurality of nozzles near from the top of the column to convert the liquid to a contaminated mist, the cylindrical column has a distance from the plurality of nozzles to the bottom that allows the mist to fall gravitationally inside the column, the air separator in fluid connection with a second vacuum source to create a vacuum with the cylindrical column, the air separator further comprises a second inlet connected to an air source, the second inlet placed in the column to allow the air from the air source to pass the mist as the mist falls gravitationally inside the column. 63. The apparatus according to claim 62, characterized in that it further comprises a gas treatment system in fluid connection with the first and second vacuum source. 64. The apparatus according to claim 62 or 63, characterized in that the second vacuum source is adapted to feed the contaminated gas from the air separator to the contaminated gas from the tank. 65. An apparatus characterized in that it comprises: an air separator in fluid connection with a contaminated water source, the air separator is in the form of a cylindrical column, the column comprises a plurality of nozzles near the top of the column for converting a liquid to a contaminated mist, the cylindrical column has a distance from the plurality of nozzles to the bottom that allows the mist to fall gravitationally inside the column, the air separator in fluid connection with a vacuum source to create a vacuum inside In the cylindrical column, the air separator further comprises a first inlet connected to an air source, the second inlet positioned in the column to allow air from the air source to pass the mist as the mist falls gravitationally into the air. column; the air separator further comprises a sump to collect the clean water that has fallen to the bottom of the column, the sump in fluid connection with a transfer pump, the sump also comprises a switch to detect the level of clean water in the sump, the switch in communication with the transfer pump and able to activate the transfer pump to remove the clean when it reaches the level; a contaminated gas treatment system in fluid connection with the vacuum source.