Water decontamination systems

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.

BACKGROUND

The invention relates to systems and methods for reducing contaminants in contaminated liquids such as contaminated ground water.

2. Description of the Related Technology

The most common sources of water contamination include but are not limited to the environmental, marine, and the petroleum industries. Water is typically contaminated with fuel hydrocarbons such as gasoline, diesel, and aviation fuel. The source of the contamination are facilities such as gasoline stations, fuel distribution terminals, underground storage tanks, military bases, airports, rail yards, shipyards, dry cleaning plants, metal plating shops, and manufacturing facilities. These facilities regularly contaminate water with volatile organic compounds (VOC's); i.e., Benzene, Toluene, Ethyl Benzene, 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. It is therefore desirable to remove such contaminants from groundwater to meet regulator standards.

SUMMARY

Described herein are embodiments of systems and methods for the purification of contaminated liquids. 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 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 are further described herein. Each of the components may be configured to operate under pressures less than, equal to, or greater than the atmospheric pressure in which the liquid decontamination system is operating.

In the foregoing embodiment, the aerator module is configured to receive the contaminated liquid. The contaminated liquid may be received from one or more contaminated sources. In a preferred embodiment, the aerator module comprises a tank to receive the contaminated liquid. In one embodiment, the aerator module comprises a plurality of nozzles which deliver a gas to the contaminated liquid. As the gas is delivered to the contaminated liquid, bubbles containing the gas form in the liquid and rise to the surface of the aerator module tank. As the bubbles pass through the contaminated liquid, the contaminants of the contaminated liquid changes phases from the dissolved contaminant into gaseous contaminants. The gaseous contaminants rise with the bubbles to the top of the aeration tank.

In some embodiments, the aerator module comprises a tank, an air distribution manifold and a compressor capable of delivering a gas or a mixture of gases such as compressed air to the air distribution manifold. In some embodiments, the tank is capable of receiving a contaminated liquid by a liquid influent connection. At least a part of the clean air distribution manifold can be contained within the tank comprising the contaminated liquid. In some embodiments, the compressor delivers air or another gas, such as ozone, to the air distribution manifold. The air distribution manifold may comprise one or more orifices which are contained within the tank through which the air is released as bubbles into the contaminated liquid contained in the tank. In some embodiments, the tank comprises baffles which create a more tortuous path for the contaminated bubbles to reach the top of the tank. The tank may be kept under a partial static vacuum to prevent leakage of gaseous contaminants to the environment. As the bubbles travel through the contaminated liquid, at least some of the contaminants in the contaminated liquid transfer phase from liquid to gas phase and are removed from the liquid as the bubble exits the contaminated liquid. This results in a contaminated gas phase in a part of the tank. The contaminated gas phase may be removed by vacuum pump.

In some embodiments, the aeration module operates under a reduced pressure. One or more vacuum pumps may be adapted to reduce the pressure of the aeration module. As the contaminants and bubbles reach the surface of the contaminated liquid, these contaminated may be transported to the one or more systems for treating gaseous contaminants by the vacuum pump. Additionally, the residence time for the bubbles in the aeration module may be increased to increase the amount of contaminants delivered to the gas phase in the aeration module. For example, the aeration tank may comprise baffles which create a more tortuous path and increased residence time for the bubbles.

In a preferred embodiment, the aeration module may 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 to a fixed level. The fixed level may be designated by a switch or detector. The switch or detector may operate a pump which 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, additional contaminated liquid may begin to fill the aeration tank. This process allows the aeration tank to operate in a continuous manner. The rates of influent and effluent contaminated liquid may be varied to adjust the flow rates of the contaminated gas and/or efficiency of the aeration module in removing contaminants from the contaminated liquid.

In some embodiments, the effluent contaminated liquid 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 combination of any of the foregoing.

In one preferred embodiment, the contaminated liquid may be passed to a separator tower module. In one embodiment, the separator tower comprises one or more atomizing spray nozzles and a tank configured to receive a liquid with reduced levels of contaminants. In one embodiment, the spray nozzles are capable of receiving the contaminated liquid and converting the contaminated liquid into a contaminated liquid mist. The tank may be operated under vacuum. Such reduced pressures may cause the liquid mist to convert 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 prior to entering the separator tower module. In one embodiment, the separator tower module may be heated. In another embodiment, the separator tower comprises packing material to increase the residence time of the liquid mist. In another embodiment, the separator tower may receive dilution air which passes over the liquid mist to further remove contaminants from the liquid mist or atomized contaminated water.

In some embodiments, the liquid decontamination system comprises a separator tower. The separator tower may comprise one or more nozzles to convert the contaminated liquid into a contaminated gas and an atomized liquid mist phase. The nozzles may be altered to determine the size and the spray of the atomized contaminated liquid. In certain preferred embodiments, the separator tower additionally comprises a vacuum chamber in which contaminated liquid is converted to a contaminated gas phase and a liquid mist phase. In some embodiments, the pressure within the vacuum chamber is about 20 inches of Hg to about 30 inches of Hg. In some embodiments, the pressure within the vacuum chamber is about 22 to about 27 inches of Hg. In one embodiments, the pressure is about 27 inches of Hg.

The separator tower may additionally comprise a sump, wherein the liquid mist may be stored, collected, or recycled back into the system. In some embodiments, the purified liquid is pumped out of the separator tower while the separator tower maintains its vacuum environment. Additionally, the separator tower may include random packing material on which the liquid mist collects into liquid droplets. These droplets may then fall into the sump and be collected. In some embodiments, a carrier (dilution) air may be used to assist transporting the contaminated gas phase out of the separator tower. A carrier air may also pass over or through the packing and/or liquid droplets and/or liquid mist phase and further remove contaminants from the liquid droplets and/or liquid mist.

The liquid phase may collect as a purified liquid in the separator tower tank. Such liquid may then be continuously pumped out of the separator tower. In some embodiments, the liquid comprising less contaminants than the contaminated liquid (the purified liquid) may fill the separator tower. At a fixed level, a switch or detector may recognize that the purified liquid has reached the fixed level and operate 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, including, but 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 may be transported to one or more systems for treating a contaminated gas. Such systems are preferably capable of removing the contaminants from the contaminated gas phase. Preferred systems for removing the contaminants from the contaminated gas phase may include one or more of electric catalytic oxidizers, thermal oxidizers, adsorption filtration systems including carbon, zeolite, and polymer adsorption filtration systems, condensers, flame oxidizers, cryogenic treatment processes, gas cooling and liquefaction processes, regenerative thermal oxidizers, and rotary concentrators.

Methods of decontaminating liquids are also described herein. One embodiment may include aerating the contaminated liquid, filtering the contaminated liquid, separating the liquid from its remaining contaminants into a contaminated gas phase and a liquid phase in a separator tower under a vacuum. Further embodiments may include treating the contaminated gas phase with a system for treating contaminated gases. Such a system is capable of reducing the levels of contaminants in the contaminated gas to a safe level wherein the gas may be released to the environment. In some embodiments, the treatment may include oxidizing the contaminants. In another embodiment, the treatment may include adsorbing the contaminants. In another embodiment, the treatment may include condensing the contaminants. Simultaneous with or after treatment of the contaminants, the remaining substantially non-contaminated gas phase is released to the atmosphere.

Another embodiment of a method comprises aerating the contaminated liquid under vacuum to separate at least some contaminants from the contaminated liquid, and purifying the contaminated gas phase released by the aerator with the system for treating the contaminated gas. According to some embodiments, this may be preformed in conjunction with the separation of a contaminated liquid into a contaminated gas phase and a liquid mist phase in the separator tower. Both contaminated gas phases may be processed in the treatment system according to some embodiments.

One embodiment of a method of reducing levels of contaminants in a contaminated liquid comprises aerating the contaminated liquid to produce a first contaminated gas phase, converting the contaminated liquid into a contaminated mist in a separator tower, converting the contaminated mist into a second contaminated gas phase and a liquid mist by subjecting the contaminated mist to a high vacuum environment within the separator tower; and treating the first and second contaminated gas phases in a treatment system. In some embodiments, the aforementioned step of treating comprises recovering the contaminants of the first and second contaminated gas phases. In some embodiments, the step of treating comprises oxidizing or reducing the contaminants of the first and second contaminated gas phases. In some embodiments, this method further comprises transporting the second contaminated gas phase out of the separator tower by vacuum. In some embodiments, this method comprises transporting the second contaminated gas phase out of the separator tower using a dilution air. In some embodiments, this method includes combining the first and second contaminated gas phases prior to treatment by the treatment system. In some embodiments, the method further includes regulating one or more steps with a controller. As discussed herein, the method may be controlled manually or automatically. In some embodiments of the aforementioned method, cleaned water is collected from the separator tower.

In another embodiment, a method of reducing levels of contaminants in a contaminated liquid includes converting the contaminated liquid into a contaminated mist in a separator tower, converting the contaminated mist into a contaminated gas and a liquid mist by subjecting the contaminated mist to a high vacuum environment within the separator tower, and reducing the levels of contaminants in the contaminated gas by a contaminated gas phase treatment system. In certain embodiments, the contaminated gas treatment system comprises an electric catalytic oxidizer. In certain embodiments, the step of converting the contaminated liquid into a contaminated mist comprises providing the contaminated liquid to an air stripper, reducing the pressure of the air stripper with a vacuum source, atomizing the contaminated liquid into a contaminated mist through a plurality of nozzles near the top of the air stripper, allowing the mist to gravitationally fall within the air stripper, and flowing air in a counter current direction to the gravitation fall of the mist. In some embodiments, method further includes controlling the rate of air flow in the air stripper 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 of reducing levels of contaminants in a contaminated liquid includes aerating the contaminated liquid in a aeration module to produce a first contaminated gas phase, transporting the first contaminated gas phase to one or more treatment systems, and reducing the levels of contaminants in the contaminated gas phase in the one or more treatment systems. In some embodiments, the method further includes collecting the contaminated liquid after aeration, wherein one or more of the contaminants of the contaminated liquid is MTBE, and wherein the step of aerating removes at least about 98 percent of the MTBE from the contaminated liquid. In some embodiments, the step of aerating the contaminated water removes at least about 99 percent of the MTBE from the contaminated liquid. Some embodiments of the foregoing embodiments include filtering the contaminated liquid. In one embodiment, the method includes receiving a second contaminated gas phase in the aeration module from a contaminated gas source, transporting the second contaminated gas phase in the aeration module to the one or more treatment systems, and reducing contaminants in the second contaminated gas phase with the one or more treatment systems. In some embodiments, the method includes mixing the second contaminated gas phase with first contaminated gas phase. In some embodiments, the contaminated gas source is the ground or soil

In one embodiment, a system includes an aerator module configured to convert one or more contaminants in a contaminated liquid into gas phase contaminants, a separator tower configured to convert the contaminated liquid into a contaminated gas phase and a liquid with reduced levels of the one or more contaminants, and a contaminated gas treatment system configured to receive the contaminated gas phase and the gas phase contaminants. In some embodiments, the contaminated gas treatment system reduces the levels of contaminants in the contaminated gas phase and the gas phase contaminants. In some embodiments, the aerator module comprises a plurality of nozzles, wherein the nozzles are configured to deliver gas bubbles to the contaminated liquid. In some embodiments, the aerator module operates under a static or dynamic vacuum. In some embodiments, the separator tower comprises a high vacuum environment. In some embodiments, the separator tower comprises a plurality of nozzles which receive the contaminated liquid and are configured to convert the contaminated liquid into an atomized contaminated mist.

In the foregoing embodiment, the contaminated mist is converted into the contaminated gas phase and the liquid with reduced levels of the one or more contaminants. 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 contaminants in the contaminated liquid. These results are further exemplified in the tables accompanying this disclosure. In some embodiment, the one or more contaminants are volatile organic compounds.

In the aforementioned embodiment, 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.

In some embodiments, the aerator module, the separator tower, and the contaminated gas treatment system is in communication with a controller. In some embodiments, the controller is capable of activating or deactivating of one or more aerator module, 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. In some embodiments, the controller is capable of regulating the influent or effluent transfer of water into or from one or more of the aerator module or the separator tower. In some embodiments, the controller is capable of regulating flow of the contaminated gas from one or more of the aerator module and separator tower.

In some embodiments, the system is configured to extract and treat a contaminated gas from soil, wherein 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 into gas phase contaminants and a contaminated gas treatment system configured to receive the gas phase contaminants. In this embodiment, the contaminated gas treatment system reduces the levels of contaminants in the gas phase contaminants.

In another embodiment, a system comprises a separator tower configured to convert a contaminated liquid into a contaminated gas phase and a liquid with reduced levels of the one or more contaminants, and a contaminated gas treatment system configured to receive the contaminated gas phase. In this embodiment, 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 a dilution air that mixes with the contaminated gas phase in the separator tower. In one embodiment, the contaminated gas phase treatment system is configured to control an amount of the dilution air.

As noted herein, in any of the embodiments, the contaminated liquid may be contaminated water.

In another embodiment of an apparatus for reducing levels of one or more contaminants in contaminated water, the apparatus includes a first container configured to receive contaminated water; the container including 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 the one or more tops walls are in contact to define an interior of the container. In some embodiments, the container also includes a first inlet in fluid connection with a contaminated water source, at least one second inlet in fluid connection with a gas source, a first outlet in fluid connection with a liquid transfer pump, and a second outlet coupled to a first vacuum source. In some embodiments, the interior is adapted to contain contaminated liquid, and the second inlet is configured to deliver a gas to the contaminated liquid. The apparatus may further include a tower in fluid connection with the liquid transfer pump, the tower further including 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 deliver the contaminated liquid to the vacuum chamber as an atomized liquid. In some embodiments, the tower may further include a bottom for receiving a cleaned contaminated liquid, and a fourth outlet located near the bottom for removing the cleaned contaminated liquid.

In some embodiments, 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 comprising a plurality of orifices configured to deliver air to contaminated water in the first container. In some embodiments, the contaminated water source is one or more means for treating water, including one or more components described herein. In some embodiments, the contaminated water source is the ground.

In some embodiments, the first container is a baffled container. In some embodiments, the first container comprises a plurality of surfaces adapted to create an indirect path for the contaminated water within the interior of the container. In some embodiments, at least some of the orifices of the gas manifold are located near the one or more bottom walls 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 openings between each chamber for allowing contaminated water to pass through said two or more chambers. In some embodiments, the gas manifold has one or more orifices for creating bubbles within one or more of the chambers, the gas manifold being in fluid connected with the second inlet.

In some of the foregoing apparatus embodiments, a means for treating a contaminated gas may further be included. Such the treatment means in fluid connection with the third outlet of the vacuum chamber. In some embodiments, a contaminated gas treatment system 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 electric catalytic oxidizer, a thermal oxidizer, an adsorption filtration system, a condenser, a flame oxidizer, a cryogenic treatment system, a gas cooling and liquefaction system, a regenerative thermal oxidizers, and a rotary concentrators.

In another embodiment, an apparatus includes a tank for containing a liquid, the tank comprising a first inlet for influent transport of the liquid, a first outlet for effluent transport of the liquid, and a second outlet for the effluent transport of a contaminated gas the tank further comprising a plurality of baffles, each baffle mounted within the tank in substantially parallel positions, wherein the liquid from the first inlet is configured to travel in one or more chambers within the tank to the first outlet, each chamber separated by at least one of the plurality of baffles, and each chamber comprising 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 outlet of the tank, the vacuum source configured to deliver the contaminated gas to a gas treatment system. In some embodiments, the apparatus includes a gas treatment system. In certain embodiments, the first vacuum source is at least a portion of a gas treatment system. For example, in some embodiments, the gas treatment system is an electric catalytic oxidizer, and the at least a portion is an oxidizer blower capable of creating the vacuum source.

In some embodiments, the apparatus may include an air stripper in fluid connection with the first outlet, the air stripper in the form of a cylindrical column, the column comprising a plurality of nozzles near the top of the column for converting the liquid into a contaminated mist, the cylindrical column having a distance from the plurality of nozzles to a bottom that allows the mist to gravitationally fall within the column, the air stripper in fluid connection with a second vacuum source for creating a vacuum with the cylindrical column, the air stripper further comprising a second 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 gravitationally falls within the column. In some embodiments, a gas treatment system in fluid connection with the first and the second vacuum source. In some embodiments, the second vacuum source is adapted to deliver the contaminated gas from the air stripper to the contaminated gas from the tank.

In another embodiment, an apparatus includes an air stripper in fluid connection with a contaminated water source, the air stripper in the form of a cylindrical column, the column comprising a plurality of nozzles near the top of the column for converting a liquid into a contaminated mist, the cylindrical column having a distance from the plurality of nozzles to a bottom that allows the mist to gravitationally fall within the column, the air stripper in fluid connection with a vacuum source for creating a vacuum within the cylindrical column, the air stripper further comprising 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 gravitationally falls within the column. In some embodiments, the air stripper further includes a sump for collecting cleaned water that has fallen to the bottom of the column, the sump in fluid connection with a transfer pump. In some embodiments, the sump further includes a switch for detecting a level of cleaned water in the sump, the switch in communication with the transfer pump and capable of activating the transfer pump to remove the cleaned water when it reaches the level. In one embodiment, the apparatus further include a contaminated gas treatment system in fluid connection with the vacuum source.

In some embodiments, the decontaminated liquid may be processed multiple times through the system for further decontamination.

DETAILED DESCRIPTION OF EMBODIMENTS

Described herein are systems and methods for separating contaminants from liquids. Contaminated liquids may include water, alcohols, hydrocarbons, oils, slurries, solutions, dissolved and melted solids, or condensed gases. In certain embodiments, water is the contaminated liquid. Some embodiments described herein are specifically in relation to contaminated water, but it may also be applicable to many other contaminated liquids.

In some embodiments, contaminated water contains contaminants which are more volatile than the contaminated water. For example, the contaminants in the contaminated water may have a boiling point that is less than that of water. Other examples include those contaminants having a higher vapor pressure than water. Contaminants may include at least one volatile organic compound (VOC). For example, contaminants may include, but are not limited to, benzene, toluene, ethyl benzene, 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 contaminants are soluble in the contaminated liquid. However, the contaminants may also be suspended in the contaminated liquid. The contaminants may also be immiscible with the contaminated liquid, and may in some cases form an emulsion.

Additionally, some embodiments of the liquid decontamination system are also capable of purifying contaminated liquid with contaminants which are solids. Contaminants may also include solids such as sediment and sand. Small particles having a diameter larger than about 0.1, 0.2, 0.3, 0.4, 0.5, 1, 2, 5, 7, 9, 12, 15, and 20 microns may also be purified by a filtration system of the liquid decontamination system. Solids may also include larger objects, and such objects may be purified from the contaminated water by sieves, filters, traps, and other similar means of filtering solids from liquids.

In another embodiment, the systems and methods as described herein are capable of purifying contaminated liquids with contaminants which are gases at standard temperature and pressure such as nitrogen. The processes such as aeration and air stripping of contaminated water may generally result in the removal from dissolved gases in the contaminated ground 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 embodiments, the system and methods employ a multi-step 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 filtering module, a separation tower module, and a contaminated gas treatment system. These component modules of a system for separating contaminants from contaminated liquids may be used together in combination. In some embodiments, only one module is necessary to remove the 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 contaminated water.

Referring toFIG. 1, one embodiment includes an aerator module10in fluid connection with the separator tower200. The aerator module is adapted to convey volatile gaseous contaminants to a contaminated treatment system201. Further the aerator module10can further convey contaminated water to the separator tower200, which can further separate contaminants from the contaminated water, and transfer those contaminants to a contaminated treatment system201. Optionally, contaminants from the separator tower may be treated by a separate contaminated gas treatment system202.

Referring toFIG. 2, one embodiment includes a separator tower200and a contaminated gas treatment system201. The separator tower200is capable of receiving contaminated water and separating at least some contaminants from the water. The contaminated gas treatment system201may then receive and treat the contaminants from the separator tower200.

Referring toFIG. 3, one embodiment includes an aerator module10and a contaminated gas treatment system201. The aerator module is capable of separating contaminants from contaminated water. The contaminated gas treatment system201may then receive the contaminants from the aerator module10.

Referring toFIG. 4, one embodiment includes an aerator module10, a filter module60, a separator tower200, and a contaminated gas treatment system201. The aerator module10may receive contaminated water and separate at least some contaminants from the contaminated water. The contaminated gas treatment system201may receive contaminants from the aerator module10. In addition, the aerator module10may then convey the contaminated water through a filter module to reduce the amount of solid contaminants, and the contaminated water may then be transferred to separator tower200. The separator tower200is capable of receiving contaminated water and separating at least some contaminants from the water. The contaminants from the separator tower200may then be transported to the contaminated gas treatment system201. In some embodiments, the contaminants from separator tower200may be combined with some contaminants from the aerator module10prior to or during treatment by the contaminated gas treatment system201.

Referring toFIG. 5, one embodiment includes aerator module10and a separator tower200. Contaminated water enters the aerator module10and is aerated which produces contaminants which exit the aerator module10. The water may then be transferred from aerator module10to separator tower200. In separator tower200, the contaminants from the contaminated water and transferred into gas phase contaminants which exit separator tower. As a result, cleaned water may be recovered from separator tower200.

Referring toFIG. 6, one embodiment includes aerator module10, two or more separator towers200, and a contaminated gas treatment system201. In this embodiment, contaminated water is aerated in the aerated module, separating at least some of the contaminants. The contaminated water may be transferred to separator tower200, where more contaminants change phase into gas phase contaminants, and the process may be repeated in the second separator tower200.

One advantage of a multi-step system is the increased efficiency in purifying contaminants from the contaminated liquid. By employing multiple components to purify a liquid, each component may selectively target a specific contaminant. For example, a liquid contaminated with solid particles and VOCs can be purified by the use of a filter module10and the separator tower200. However, in some preferred embodiments, a system comprising an aerator module10, a filtering module60, a separator tower module200, and a contaminated gas treatment system201provides an efficient method of 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 aerator10, filter60, separator tower200, and a contaminated gas treatment system201is provided below. A contaminated liquid may be introduced into an aeration tank10comprising an aeration compressor20. Such aeration compressor20operates to produce small bubbles that rise through the contaminated liquid into the headspace12of the aeration tank10. Bubbles introduced to the contaminated liquid carry contaminants from the contaminated liquid into the headspace12of the aeration tank10. Additionally, an aeration tank11may comprise baffles 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 the increased efficiency in the removal of contaminants by the aerator module10. These contaminants are then transferred out of the aeration tank10with the contaminated air and processed by the contaminated gas treatment system201. In some embodiments, the aerator module operates under a static or dynamic vacuum to prevent the egress of contaminants. The contaminated gas treatment system201may release the purified gas stream as environmentally safe exhaust into the atmosphere, or may otherwise trap the contaminants.

In some embodiments, liquids which have been processed by the aerator module10may be transferred to one or more other treatment modules201,202. In one embodiment, the contaminated liquid may be transferred to at least one filter module60. In some embodiments, a liquid transfer pump is used to transfer liquid from the aerator module10to a filter60. 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 which are contaminants and/or those solids that could potentially foul equipment down stream of the filter. Optionally, filter modules60may be placed prior to the aerator module10, or both prior to and after the aerator module10.

In some embodiments, the contaminated liquid may be transferred to a separator tower module200. In some embodiments of this module, the liquid enters a sealed vacuum chamber through at least one atomizing spray nozzle. The liquid is thus converted into a mist. The vacuum environment converts the contaminated liquid mist into a contaminated gas phase and a liquid mist phase. The pressure inside such a chamber may vary, but includes from about 20 inches of HgG to about 30 inches of HgG, and more preferably about 26 inches of HgG. In one embodiment, the pressure is about 2 PSIA. The vacuum environment can be tuned depending on the contaminants and the liquid to be decontaminated, and thus be less than 20 inches or greater than 30 inches of HgG. One example of a vacuum pump that may be used is the Siemens 2BL-8.3 HP Vacuum Pump Unit.

The contaminated gas phase can then be carried away by the vacuum pump. Additionally, the liquid mist can pass over optional random packing, thus exposing the mist to more surface area within the separator tower200. To assist in the removal of the gas phase contaminants, carrier air can be added to the separator tower200. The carrier air passes over the packing material that has exposed more surface area of the liquid mist, thus removing any remaining contaminants of the liquid mist phase. The dilution air comprising the contaminants is then carried toward the vacuum pump. In some embodiments, the rate and amount dilution air can be controlled to increase the efficiency of removing the contaminants from the contaminated water in the separator tower200

The liquid mist may collect into liquid droplets. These droplets may collect in the bottom portion of the separator tower (also know as the sump). The liquid may be pumped out of the separator tower into a storage tank. In some embodiments, the liquid can be taken directly from the separator tower. Such liquid may subjected to one or more other treatment means, including the modules as described herein.

In some embodiments, the liquid may container less than 10% of the targeted contaminants of the 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 targeted contaminants of the contaminated liquid. In preferred embodiments, the purified liquid contains less than 1% of the targeted contaminants including about 0.0001%, 0.001%, 0.01%, 0.5%, 0.1%, and 0.5%, and values between the foregoing.

In some embodiments, the contaminated gas phase and the carrier air (also referred to herein as the dilution air) are carried out of the separator tower. In some embodiments, these gases pass through the process gas blower. Optionally, the contaminants may also pass through a contaminated gas treatment system. Such systems are further described herein.

The modules and certain embodiments are further described below as they relate to the accompanying figures. However, this is in no way intended to limit the scope of the invention which is defined by the claims that follow.

Aerator Module

FIG. 7represents one nonlimiting example of an aerator module10. Contaminated liquid13enters the aeration tank11at liquid influent connection point15. The contaminated liquid influent connection point15is located above the static contaminated liquid level in the aeration tank10. However, in some embodiments, liquid influent connection point15can be located in other locations within the aeration tank11. In some embodiments, the influent connection point15is located above the level of the contaminated water13. This advantageously allows contaminated water13to be treated by aerator module10and transported away from aeration tank11at effluent connection point45. In some embodiments, the contaminated water13may be sprayed into the aeration tank11to further increase the efficiency of removing contaminants from the contaminated water13.

The aeration tank11is in communication with aeration compressor20. Aeration compressor20is configured to deliver compressed gases to the aeration tank11by way of a gas distribution manifold25. In some embodiments, aeration compressor20continuously delivers air or other gases into the gas distribution manifold25. It may provide the selected gases, such as air, to the contaminated water13at a sufficient pressure to effect bubbling in the contaminated water13in aerator tank11. In some embodiments, air may be delivered to the aeration tank11by a compressed air source. In some embodiments, gases such as ozone can be used in the purification of water during the aeration process. In some embodiments, aeration module10may also comprise an ultraviolet light purification system. In some embodiments, the air filter60is used to purify incoming air from the air compressor20.

In some embodiments, the gas distribution manifold25may be attached to the bottom of the aeration tank11. Aeration compressor20is connected to the aeration tank11via pipeline66. Pipeline66connects to the gas influent connection point55near the base of aeration tank11. Gas distribution manifold25may be further connected to the pipeline66to the gas influent connection point55. In some embodiments, the pipeline66is fitted with a check valve65, manual ball valve70, and a pressure gauge75. Check valve65is designed to prevent the flow of gas from the aeration tank11back through the aeration compressor20. Manual ball valve70is closed it enables servicing of the aeration compressor20and check valve65. Pressure gauge75indicates the clean air pressure entering the aeration tank11. Manual ball valve80enables servicing of pressure gauge75.

The gas distribution manifold25may comprise a plurality of pipelines which extend the length of the aeration tank11. Gas distribution manifold25may be attached to the bottom of the aeration tank10or configured to be near the bottom of aeration tank11. In some embodiments, the gas distribution manifold25comprises a plurality of orifices30. In some embodiments, the gas distribution manifold is perforated with orifices several times per inch. The size of the orifices may vary depending on the application, and pressure. In some embodiments, the orifices are generally small in diameter. As the gas distribution manifold25is pressurized by the aeration compressor20, gas exits the clean air distribution manifold25through orifices30. Orifices30cause the gases, such as compressed air, to form small bubbles as the clean air exits the clean air distribution manifold25and enters the aeration tank11. The small bubbles exit the clean air distribution manifold25and rise through contaminated liquid13in the aeration tank11. As the bubbles rise through the contaminated liquid13, some of the contaminant transfers from the contaminated liquid into the bubbles.

Aeration tank11may be made of different sizes, shapes and materials. In one embodiment, aeration tank11may be constructed of stainless steel or other materials suitable for containing the contaminated water13. In some embodiments, aeration tank11may hold up to 1000 gallons of contaminated water, including about 50, 100, 200, 300, 400, 500, 600, 700, 800, 900 and 1000 gallons. Ranges between, below, and above such values gallons of are also contemplated.

Referring toFIG. 8, in some embodiments, aeration tank11contains a series of internal walls or baffles23. Contaminated liquid13enters tank11at influent connection point15and flows over and under the wall, which create a tortuous path for the water. The tortuous path increases the residence time of the contaminated liquid13in the aeration tank11. Increasing the residence time allows for more contaminants in the liquid to transfer into the bubbles generated by the aeration compressor20and the gas distribution manifold25. The contaminants are then transferred to the headspace19of tank11. This is one method increasing the amount of contaminants that can transfer from liquid phase to gas phase while in the aeration tank11. Once these contaminants are in the gas phase they are removed from the aeration tank11and destroyed by a contaminated gas treatment system.

Additionally, in some embodiments, walls are added to the aerator module to make the pathway for the bubble more tortuous, thereby increasing residence time. When the bubbles reach the surface of the contaminated liquid they collect in the headspace19at the top of the aeration tank11. The aeration tank11may be fitted with an air tight lid14to prevent the gaseous contaminants from escaping into the atmosphere. In one embodiment, the head space19is connected to a vacuum pump. In another embodiment, head space19of aeration tank11is connected to the negative pressure side of the process gas blower510via a pipeline. The pipeline is fitted with an automatic vacuum control valve51. The automatic vacuum control valve51ensures that a steady state vacuum is maintained in the headspace19of the aeration tank11. In some embodiments, the gaseous contaminants travel into a contaminated gas phase treatment system201. The contaminated gas phase treatment system may be specifically designed to oxidize, adsorb, and/or condense the target contaminants in the gas phase. Such gas phase treatment systems are further described herein.

Other means for increasing the residence time of the bubbles and the efficiency of the aerator tank may also be used. In another embodiment, the aeration tank or the water inside of the aeration tank may be heated. Without wishing to be bound to any particular theory, heating the aeration tank or the water inside of the aeration tank may increase the efficiency of the overall process of decontaminating the water. In some embodiments, a heat exchanger may be used to heat the contaminated liquid13prior to, during, or after the aeration tank module. In some particular embodiments, the heat exchanger may exchange heat given off by another component of the liquid decontamination system. For example, a heat exchanger may 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 embodiments, the water is heated to a temperature ranging between about 50 to about 105° F. In another embodiment, the water is heated to a temperature ranging between about 80 to about 100° F.

In addition, the vacuum pressure maintained in the aeration tank may also be controlled. In some embodiments, the vacuum pressure is static and produced a vacuum. In some embodiments, the vacuum is dynamic. In some embodiments, the pressure is lower than atmospheric pressure. In some embodiments, the pressure is about 680 to 760 Torr. In some embodiments, the pressure is about 740 to about 760 Torr. In some embodiments, the vacuum pressure is dependent on the temperature of the contaminated liquid13.

In one embodiment, the aeration tank11will receive contaminated gases directly from a contaminated source. These gases may or may not be dissolved in a contaminated liquid13. For example, it will be understood to those having ordinary skill in the art that the liquid decontamination systems described herein may operate in a dual phase capacity. As such, the contaminated gases delivered to the aeration module10, or any other module of the water decontamination system, may pass directly to the contaminated gas treatment system201by the delivery means as described herein. In one embodiment, the effluent connection inlet is configured to be above the contaminated water level such that the contaminated gases, which are delivered to the aeration module, pass directly to the headspace19of the aeration tank10. From the headspace19, the contaminated gas phase may be delivered to the contaminated gas treatment system201via the vacuum or other means.

In some embodiments, the aeration module10may be operated continuously and/or automatically. In one embodiment, aeration tank11is equipped with liquid level control35and a high level alarm shut down switch85. As contaminated liquid fills the aeration tank11the contaminated liquid level is continuously monitored by liquid level control35. At a field settable contaminated liquid level the liquid level control35activates and sends a pump start signal to a programmable logic controller in a control panel. The programmable logic controller then sends a signal to start contaminated liquid transfer pump90. While the foregoing is described as a programmable logic controller, other manual and automatic means of signaling the transfer pump are known and are contemplated herein. Such automated systems are also further described herein.

In one embodiment, contaminated liquid transfer pump90starts and pumps the contaminated liquid13away from the aerator tank11. Contaminated liquid transfer pump90may pump the contaminated liquid to one or more other treatment modules of the water decontamination system, such as the filtration system or the separator tower. If the contaminated liquid transfer-pump90fails to start, or fails to prime, or if the aeration tank10is filling too rapidly, the contaminated liquid level will continue to rise in aeration tank10. The rising contaminated liquid level in aeration tank10will eventually reach the high level alarm float switch85. At the high level alarm point the high level alarm float switch85activates and sends a signal to the programmable logic controller in the control panel. The programmable logic controller then shuts down the system and stops the flow of contaminated liquid into aeration tank10.

FIG. 8Ashows an exploded view of one configuration of an aerator module. Aerator tank11is made from four side walls,391A,391B,391C,391D and bottom wall392. The walls may be attached together by any means to form a box, including, but not limited to, being welded together on the respective sides of each wall. Side wall391C includes an influent connection point15in which contaminated water is allowed to pass into aeration tank11. Side wall391A includes effluent connection point45in which contaminated water is allowed to pass away from the aeration tank. Side wall391B includes opening contaminated gas effluent connection point50. Side wall391D may be outfitted with drain valves397to allow drainage of the aeration tank11.

Placed within the tank formed by the side walls391A-D and the bottom wall392are the gas distribution manifold25. The gas distribution manifold25includes the gas influent connection point55, which may be connected to an air compressor, or other gas delivery system. Gas distribution manifold comprises a plurality of orifices30, which are 0.5 inch half nipples. However, as discussed above, the size of the orifices30may vary.

Also within the aeration tank are baffles23A,23B,23C,23D, and23E. These baffles create a tortuous path for the water as it enters the aeration tank11. As shown, some baffles, such as baffles23B,23D, and23E may contain openings399,398for water to pass through as the water fills each respective chamber of the aeration tank. Alternatively, the baffles, such as baffles23A and23C may be oriented to allow water to pass under the baffles. The orientation of the respective chambers is further shown inFIG. 8B

As previously noted, the aeration tank11may operate under vacuum. Flange394may be welded to side walls391A,391B,391C, and391D. In some embodiments, the flange may also be welded to the baffles23A,23B,23C, and23D. Air tight lid14may be bolted to flange394. In some embodiments, the air tight lid14is made of steel.

Furthermore, in some embodiments, the bottom wall392may be attached to flange395, which is then further connected to base396. Base396allows for the aeration tank to not be placed on the ground. Base396also includes slots401which allow the aeration tank11to be easily moved by equipment that can manipulate the base using the slots, such as a forklift.

As an illustration, water that enters the aeration tank11at influent connection point15must pass under baffle23A. At the same time, compressed air may be pumped into the aeration tank11via the manifold25and orifices30. As the water fills the tank11from the influent connection point15, the water will rise to a level such that it reaches the height of openings399in baffle23B. Water then will fill the next chamber of the aeration tank and then be forced under baffle23C and into the next chamber. The level of the water will then rise to the height of the openings399of baffle23D and pass through the openings399of baffle23D. After passing baffle23D, water then must fill the next chamber before reaching opening398. As shown in the figure, the water will then fill the final chamber of the aeration tank11. Water then may be removed by way of effluent connection point45in side wall391A. In some embodiments, the last chamber may be outfitted with a float switch or other mechanism which automates the liquid transfer pump90and removes the contaminated water by way of liquid effluent connection point45.

FIG. 8Bpresents a front view of the aeration tank fromFIG. 8A. As shown the aeration tank may be divided into multiple chambers by baffles23A,23B,23C,23D, and23F. As shown, baffles23A and23C are not connected to bottom wall392, which allows water to pass under baffles23A and23C. As further shown baffles23B,23C,23D are contact bottom wall392and top lid14, allowing water to only pass through openings in the respective baffle. Gas distribution manifold25may be configured to pass through each respective baffle at a different opening than the water passes through. Further, gas distribution manifold25possess a number of appendages which deliver air to the respective chambers through orifices30.

Referring toFIG. 8B, the chambers as divided by baffles23A,23B,23C, and23D. The chambers may be equal or different sizes. In one embodiment, each of lengths a, b, c, d, e, and f independently ranges from about 6 to about 40 inches. In one embodiment, each length a, b, and e is about 12 inches, each length c and is about 18 inches, and length e is about 28.5 inches. However, these lengths may vary according to the size, dimensions, and desired flow rates of the contaminated water. Height g may range from about 30 to about 60 inches. In some embodiments, height g is about 50 inches.

Referring toFIG. 8C, this side view of aerator tank11shows the manifold25which delivers air through orifices30. It also shows openings399in a baffle. In some embodiments, length i ranges from about 20 to about 40 inches, including about 25, 26, 27, 28, 29, 30, 31, and 32 inches. Furthermore, a top view of the aerator tank11is shown inFIG. 8D. Length h may range from about 60 to about 150 inches. In some embodiments, length h is ranges from about 80 to about 120 inches. In one embodiment, length h is about 100 inches.

Transfer Pump & Filter Module

As discussed above, some embodiments of systems may include a transfer pump90to transfer contaminated water from one component to another. Referring toFIG. 9, in one embodiment, transfer pump90may transfer contaminated water from aeration module10to a filtration module300. Contaminated liquid transfer pump90may be connected to aeration tank10by pipeline107. In one embodiment, the pipeline107is connected to the aeration tank10near the bottom of the final chamber at the effluent connection point45.

In some embodiments, the pipeline may be equipped with ball valves105and110and y-strainer120located on the upstream side of the contaminated liquid transfer pump90. Closing the ball valves105and110enables servicing of y-strainer120. Y-strainer120is designed to remove solid particles larger that twenty microns from the contaminated liquid. However, other filters may be used in place of Y-strainer120. In some embodiments, no filter is necessary because the contaminated water was prefiltered. Filtered water prevents damage to the contaminated liquid transfer pump90. However, the sizes of the filter may vary and solid particles can be larger or smaller than about 20 microns, including about 5, about 10, and about 15 microns can be removed.

Contaminated liquid transfer pump90may be any type of pump. In one embodiment, contaminated liquid transfer pump90is a centrifugal pump. To obtain continuous flows, a five horsepower pump may be used for 10-15 gpm system. A larger pump may be used on a system with increased flow and production rates of water. Thus, the size and power of the contaminated liquid transfer pump may vary according to the total output of the liquid decontamination system. One example of a suitable transfer pump is the Transfer Pump, 1.5HP, TEFC, 3 Phase, available from Price Pump Co. (Part No. CD100BF-450-6A212-150-353T6). Another suitable transfer pump includes are Gould Pumps (G& L Series Model NPR/NPE-F), available from ITT Water Technology, Inc.

In one embodiment, ball valves110and125are located upstream and downstream of the contaminated liquid transfer pump90to enable servicing of the contaminated liquid transfer pump90.

Further referring toFIG. 9, the contaminated liquid transfer pump90is connected to the separator tower200by a pipeline. As shown in the embodiment of the figure, the pipeline is equipped with four ball valves125,130,135,140, one check valve145, three sample ports150,155, and160, three pressure gauges165,170, and175, and two filter housings180and190. Check valve145is designed to prevent the back flow of liquid from the separator tower200to the aeration tank10. Ball valves125and130enable servicing of check valve145.

As further noted inFIG. 9, the contaminated liquid transfer pump90may transfer the contaminated water13to a filtration module300. Filtration module300may include one or more filters to reduce contaminants 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 fitted with more than two filter housings. These filter housings may be used in series or may be used separately for two different sources of water. One nonlimiting example of a filtration module is shown inFIG. 9. In this example, the filtration module includes primary filter housing180and secondary filter housing190. Each of primary filter housing180and secondary filter housing190may include a solid filter element. In some embodiments, each of primary filter housing180and secondary filter housing190may be equipped with about 5 to about 25 micron filter element. In one embodiment, the primary filter element180is equipped with a 10 micron filter element and the secondary filter housing190is fitted with a five micron filter element. In some embodiments, the filters can filter particles of different sizes or the same size. The particles which may be filter includes particles having a size of 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 Model NCO Bag of Cartridge Filter Housings available from Rosedale Products, Inc. (Part No. NC08-15-2P-*-150-C-V-PB).

Referring toFIG. 9, some embodiments include ball valves130and135which enable servicing of primary filter housing180, and ball valves135and140which are upstream and downstream of secondary filter housing190. In some embodiments, pressure gauges165and170are used to determine the service interval of the bag filter elements in primary filter housing180, and pressure gauges170and175are used to determine the service interval of the bag filter element in the secondary filter housing. The difference between the upstream pressure gauge and downstream pressure gauge readings indicates the condition of the bag filter element in primary filter housing180. Ball valves205,210enable servicing of the pressure gauges. Balls valves135and140enable servicing of secondary filter housing180. Ball valves140and235enable servicing of175.

Continuing to refer toFIG. 9, some embodiments include sample ports150,155, and160. In these embodiments, sample ports150,155,160enable the collection of contaminated liquid samples. Such samples are used to determine the effectiveness of the system and process. In addition, filtration system300may be equipped with a contaminated liquid temperature gauge220and a contaminated liquid flow meter230. Ball valves235and240enable servicing of the contaminated liquid flow meter230.

Separator Tower Module

One effective mode of removing contaminants such as VOCs or halogenated organic compounds from water is through an airstripping process. In some embodiments, the water decontamination system includes a separate tower module200. In some embodiments, the separator tower200acts an air stripper which produces a phase change of contaminants which are dissolved in the contaminated water. At least some of the contaminants in the contaminated water change phases from liquids to gases in the separator tower200. In some embodiments, contaminated liquid is pumped into the separator tower200near the top of separator tower200. Spray nozzles260create small droplets of contaminated liquid which increases the amount of surface area of contaminated liquid exposed to the dilution air. The atomized contaminated liquid is then exposed to reduced pressures in separation tower200and the contaminants change from liquid to gas phase. As the small droplets of contaminated liquid fall in separator tower200, the contaminants change phase

Referring toFIG. 10, in some embodiments, the contaminated water is sprayed through a plurality of spray nozzles260into the separator tower200which is under vacuum. The plurality of spray nozzles260may comprise atomizing spray nozzles. Spray nozzles260may be configured and arranged as to provide an efficient conversion of the contaminated liquid into a contaminated mist.

For example,FIG. 11demonstrates one arrangement of spray nozzles260in separator tower200. Spray nozzles260are arranged on a spray nozzle manifold261. In some embodiments, spray nozzle manifold is in fluid connection with influent connection point250. Spray nozzle manifold may come in many different configurations. In one embodiment, the spray nozzle manifold comprising the plurality of nozzles may be located on a cartridge. Such a cartridge may be replaceable in the separator tower200

In some embodiments, separator tower200comprises about 20 to about 40 atomizing spray nozzles260. In some embodiments, separator tower200comprises about 10 to about 50 atomizing spray nozzles260. In some embodiments, spay nozzles260are located at near the top of separator tower200and spaced evenly apart from one another. Suitable spray nozzles260include nozzles having a size of about 4 to about 5 microns. The size however is variable as noted above and is not limited to the described sizes, and also includes from about 1 to about 5 micron sized nozzles, and from about 5 to about 20 micron sized nozzles.

The pressure of the atomized contaminated water at the plurality of nozzles may be varied according to flow rate of the contaminated water, the number of nozzles, and the size of the orifices of the nozzles. In some embodiments, the pressure of the fluid at the nozzles is between about 10 to about 150 PSIG. In some embodiments, the pressure of the fluid at the nozzles is between about 20 to about 80 PSIG. In some embodiments, the pressure of the fluid at the nozzles is between about 40 to about 65 PSIG.

In some embodiments, the nozzles260of the separator tower200may be optionally heated. Methods of providing heat to the spray nozzles260are known in the art. One method comprises providing electricity to the nozzles while grounding the nozzles260to eliminate any charge. The nozzles may also be attached to a thermocouple to control heating of the nozzles.

In one embodiment, a vacuum pump510is adapted to connect to the separator tower200near the top of the separator tower200at the effluent connection475. In one embodiment, the spray nozzles are placed at a level below the vacuum inlet475. In one preferred embodiment, the vacuum inlet475is about 2 to about 7 inches below the top of the separator tower. In this embodiment, the spray nozzles are about 2 to about 10 inches below the vacuum inlet. In some embodiments, the spray nozzles may be located further below the vacuum inlet than then prescribed ranges.

In some embodiments, a static or dynamic vacuum is maintained inside of separator tower200by vacuum pump510. In one embodiment, a dynamic vacuum is preferred. A high vacuum can reduce the pressure of the separate tower module200to provide a low energy, high vacuum environment to assist in the interphase transfer of the contaminants. The reduced pressures in the separator tower200increase the volatility of the contaminants in the contaminated water. In some embodiments, separator tower200is operated under a high vacuum. The exact pressure of the chamber may vary depending on the contaminants. In some embodiments, the pressure is about 27 inches of Hg, but this may vary. In some embodiments, the pressure is about 10 to about 40 inches of Hg. In some embodiments, the separator tower operates under a high vacuum. Referring toFIG. 10, ball valve415may be manipulated to obtain the proper operating pressure of the separation tower200at pressure gauge263. Pressure gauge263may also be controlled automatically by a programmable logic controller on the control panel or read manually.

In some embodiments, carrier or dilution air can be passed over the contaminants to transfer as much of the contaminants from the liquid phase to the gaseous phase. The contaminated gas phase may mix with the dilution air prior to, during, or after the phase change of the gaseous contaminants. In some embodiments, the rate of dilution air can be controlled to increase the efficiency of the transfer of the contaminants from the liquid to the gas phase. In some embodiments, the dilution air flow rate may be varied from about 0.1 to about 20 SCFM. In some embodiments, the dilution air flow rate may be varied from about 0.5 to about 15 SCFM. In some embodiments, the dilution air flow rate may be varied from about 1 to about 10 SCFM. The dilution air may be maintained at any flow rate value between the aforementioned rangers. The term “SCFM” means Standard Cubic Feet per Minute, referenced to a pre-specified pressure, temperature, and relative humidity. As used herein, SCFM is referenced to 14.7 PSIA, 68° F., and 0% relative humidity. Alternatively in some embodiments, dilution air is not required to effect transfer of the contaminants from the liquid phase to the gas phase.

Referring toFIG. 10, in one embodiment, dilution air enters the separator tower200at the dilution air filter410. The flow rate of the dilution air may be controlled manually or automatically. For example, the dilution air may be controlled by a programmable logic controller in the control panel. In some embodiments, ball valve415is used to control the flow of dilution air into separator tower200. In some embodiments, dilution air flow meter420indicates the flow rate of dilution air entering the separator tower200.

In one embodiment, dilution air enters the separator tower200near the mid point of sump280However, other embodiments allow for the dilution air to enter the separator tower at other locations in the sump280or above the sump280. Dilution air flows up through the sump280, optional random packing270and mixes with the contaminated gas phase. Once the dilution air mixes with the contaminated gas phase, the mixture continues upward in separator tower200to the process gas effluent connection475. Upon exiting the separator tower200the process gas passes through the vacuum pump510and process gas blower and enters the contaminated gas phase treatment system201.

In some embodiments, the residence time of the atomized contaminated water may be increased by filling the separator tower200with optional random packing270. Random packing270increases the amount of surface area inside the separator tower200. One or more supports may be used in the separator tower to support such packing material. Random packing support grid285may be installed to prevent the random packing from falling into the separator tower sump280. Examples of suitable packing include Jaeger Tri-Packs®, but are not limited thereto. In some embodiments, no packing is used.

In some embodiments, the contaminated water may be heated to further increase the efficiency of the phase change of the contaminants in separator tower. In some embodiments, the water may be heated by the spray nozzles. In other embodiments, the water is heated prior to entering separation tower200. In some embodiments, the water is heated from heat from other components of the water decontamination system, such as a heat exchanger on the one of transfer pump (e.g., transfer pump90), vacuum pump510, or contaminated gas treatment system201. In some embodiments, the temperature of the contaminated water may be maintained in the range from about 40 to about 150° F. In some embodiments, the temperature of the contaminated water may be maintained in the range from about 60 to about 110° F. In some embodiments, the temperature of the contaminated water may be maintained in the range from about 70 to about 100° F.

As noted above, the dimension of the separator tower module may vary with the type, amount and concentration of contaminant(s), the volume of water to be processed by the separator tower, the desired flow rates through the device, and the desired pressures in the vacuum chamber of the separator tower. In some nonlimiting embodiments, the separator tower is a cylindrical. In some embodiments, the separator tower has a storage capacity of about 20 to about 5000 gallons of liquid. In some embodiments, the storage capacity of the separator tower is about 100 to about 1000 gallons. In another embodiment, the storage capacity of the separator tower is about 80 to about 200 gallons. In a preferred embodiment, the separator tower has a capacity of about 100 gallons.

The shape and dimensions of the separator tower may vary. In one embodiment, a cylindrical separator tower module is about 3 to about 20 feet tall (1 meter to about 6 meters). In another embodiment, the separator tower is about 6 to about 30 feet tall (2 meters to about 10 meters). In one preferred embodiment, the separator tower is about 12 feet tall.

As the separation process occurs in the separator tower200, purified water comprising less contaminants than the contaminated water falls to the bottom of the separator tower200. In some embodiments, the cleaned water may be produced at a rate of between about 1 to about 20 gpm. In some embodiments, the cleaned water is produced at a rate of between about 5 to about 15 gpm. In some embodiments, the cleaned water is produced at a rate of about 10 gpm. However, different configurations and scale of the liquid decontamination system may allow for production of water at rater rates than 10 gpm, including up to about 200 gpm.

In some embodiments, the cleaned water collects and begins to fill sump280. Sump280can be drained and/or pumped out. This process can occur continuously or in a batch process. This process may also occur manually or automatically. In some embodiments, sump280may be equipped with a manual drain valve315to drain the cleaned water from the sump. In other embodiments, cleaned water effluent connection320is located near the bottom of the sump280. Cleaned water effluent connection320is connected to the clean liquid transfer pump310by a pipeline281.

In some embodiments, sump280of separator tower200may be equipped with a pump down float switch290and a high liquid alarm float switch295. The rising liquid level in sump280is monitored by the pump down float switch290, which may be monitored manually or automatically. In one embodiment, the float switch activates at a field settable clean water level, and sends a start signal to cleaned water transfer pump310. These switches and pumps may be monitored and/or activated by a programmable logic controller in the control panel. If the cleaned water transfer pump310fails to start, fails to prime or fails to pump and the cleaned liquid level continues to rise in the separator tower sump280the cleaned liquid level will eventually reach the high level alarm point295. At the high level alarm point295, the high level alarm float switch activates and sends a signal to the programmable logic controller in the control panel to shut down at least a part of the process.

In some embodiments, pipeline281is fitted with one or more ball valves325,330,335,340,345,350, one or more y-strainer355and one or more check valves360,365, one or more sample ports370and one or more clean water flow meter380. Y-strainer355may be used to remove solid particles, including those larger than twenty microns. Ball valves325and330allows for servicing of y-strainer355. Check valve360is designed to prevent cleaned water from flowing back into separator tower200. Check valve365is designed to prevent clean liquid from flow back into the cleaned water transfer pump310. Ball valves330and335allows for servicing of check valve360. Ball valves335and340allows for servicing of cleaned water transfer pump310. Ball valves340and345allows for servicing of check valve365. Ball valves345and350allow for servicing of the clean liquid flow meter380.

In some embodiments, cleaned water effluent connection390may be connected to a holding tank, storm drain or other method of controlling the clean liquid pumped out of system. In some embodiments, the cleaned water may be recycled to one or more components of the water decontamination system. In one embodiment, the cleaned water may be transported back to separator tower200for further processing. In another embodiment, cleaned water may be processed by one or more second separation towers, which are similar to or different from separator tower200. In some embodiments, the cleaned water may be recycled to the aeration module10, or different aeration modules. In addition, cleaned water may be processed by one or more other treatment methods, such as passing the cleaned water through an activated carbon filter. A person having ordinary skill in the art will understand many of ways of further processing the contaminated water by one or more of the components of the water decontamination system as described herein or other decontamination processes, such as municipal treatment processes.

Contaminated Gas Phase Treatment Systems

In some embodiments, the contaminated gas phase is transferred to a contaminated gas phase treatment system201. In one embodiment, the liquid decontamination system comprises one or more contaminated gas treatment systems201,202. The one or more contaminated gas treatment systems may reduce the levels of contaminants in the contaminated gas. In one embodiment, the contaminated gas phase is transferred from the aerator module10to the contaminated gas phase treatment system201. In another embodiment, the contaminated gas phase is transferred from the separator tower200to the contaminated gas phase treatment system201. In some embodiments, the contaminated gas phases from the separator tower200and the aerator module10are transferred to the contaminated gas phase treatment system201. This transfer may occur at the same time, which causes the contaminated gas phases from the aerator module10and the separator tower200to mix prior to treatment. However, these contaminated gas phases may be treated separately by one or more treatment systems.

In certain embodiments, the contaminated gas phase is treated so that a gas phase comprising substantially no contaminants can be released to the environment. The contaminants from the contaminated gas phase may be trapped or transformed into other compounds which 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 system201is configured to remove or change the gas phase contaminants from other gases which can be expelled from the system as exhaust. In some embodiments, the gas phase contaminants are oxidized. In one embodiment, the contaminated gas phase contaminants are converted into carbon dioxide and water.

The oxidized contaminants may then be released to the atmosphere. In another embodiment, the gas phase contaminants are condensed. Other process gases, such as the remaining dilution air, as well as other environmentally safe compounds, may be released to the atmosphere. In another embodiment, the gas phase contaminants are adsorbed. The remaining dilution air and nonadsorbed gases may be released to the atmosphere. Furthermore, the contaminated gas phase may be subjected to one or more treatment systems to rid the contaminants from the gas phase.

The one or more contaminated gas phase treatment systems201may vary according to the contaminants. Suitable contaminated gas phase treatment systems include, but are not limited to, one or more of electric catalytic oxidizer (seeFIG. 12), thermal oxidizers, adsorption filtration systems (seeFIG. 13) including carbon, zeolite, and polymer adsorption filtration systems, condensers (seeFIG. 14), flame oxidizers, cryogenic treatment processes, gas cooling and liquefaction processes, regenerative thermal oxidizers, and rotary concentrators. Some of these treatment systems are further described herein.

Some contaminated gas phase treatment systems201may be limited in the amount or rate of gaseous contaminants that it receives and/or treats. In addition, the amount of exhaust which may be released is often determined by environmental regulations governing compounds in the exhaust. Similarly, such contaminated gas phase treatment systems201may also be limited in the release of byproducts of such treatment processes to the atmosphere. To regulate the amount and concentration of contaminants subjected to treatment in the contaminated gas phase treatment system201, the flow rates of the contaminated gas phase may be controlled.

For example, the amount of dilution air received with the contaminants may be controlled. As described above, the dilution air may be mixed with the contaminated gas phase in the separator tower module200. However, the dilution air may also be mixed with the contaminated gas phase outside of the separator tower200. In some embodiments, the treatment system201may require additional dilution air to process the contaminated gas phase. In such instances, the treatment system201may signal the dilution air valve415to allow an increase of dilution air to enter the contaminated gas phase. Such signaling may occur manually or automatically based on a programmable logic control in the control panel.

In some embodiments, the contaminated gas treatment system201may detect an amount or concentration of contaminant which exceeds that allowed by regulation. Exceeding such levels may require further dilution or shut down the liquid decontamination system. In one embodiment, one or more components of the liquid decontamination system may discontinue the further processing of one or more of the contaminated gas, contaminated liquid, purified gas, dilution air, or the decontaminated liquid. In some embodiments, the cease of one or more of the aforementioned components, may allow the treatment system to reduce the levels of contaminants. When the system detects that one or more of the contaminants has reached a designated and/or safe level, or a level prescribed by environmental laws, then the system may optionally restart one or more components of the liquid decontamination system.

Several examples of certain treatment systems are described below:

Electric Catalytic Oxidizer

Some liquid decontamination systems as described herein comprise a catalytic oxidizer module. In some embodiments, the catalytic oxidizer is an electric catalytic oxidizer100. In some embodiments, the catalytic oxidizer module100may receive a contaminated gas phase from the separator tower200. In some embodiments, the catalytic oxidizer module receives a contaminated gas phase from the aerator module10. In certain embodiments, the catalytic oxidizer module100receives more than one contaminated gas phase, including the contaminated gas phases from the aerator module10and the separator tower200. This process may remove up to 99.99% of the targeted contaminants and produce exhaust that may be released to the environment.

Embodiments of catalytic oxidizers may vary. Referring toFIG. 12, some embodiments of catalytic oxidizers will include a catalyst570. Other embodiments include a heater560which heats the contaminated gas phase prior to introduction to the catalyst570.FIG. 12represents a nonlimiting example of an electric catalytic oxidizer module100. The electric catalytic oxidizer100is equipped with an oxidizer blower520, flame arrestor530, pitot tube540, air to air heat exchanger550, electric heater560, catalyst570and an exhaust stack580. The electric catalytic oxidizer100is also equipped with pressure switches, temperature switches, and temperature sensors for controlling the process of oxidizing the process gas. The process gas passes through a pipeline511to the electric catalytic oxidizer100. The process gas enters the electric catalytic oxidizer100through the null hood590at oxidizer blower520. The null hood590may balance the amount of contaminated gas phase and dilution air entering electric catalytic oxidizer100. In some embodiments, the null hood590in conjunction with the oxidizer blower520balance the dilution air and process gas to ensure that the temperature of the process gas/dilution air is at the correct temperature at it approaches and as it is treated by the catalyst. Thus, these components may prevent a high temperature alarm605in electric catalytic oxidizer100. In some embodiments, the oxidizer blower blows the process gas and an additional dilution air at flow of up to 200 SCFM, including about 50, 100, and 150 SCFM.

Referring toFIG. 12, flame arrestor530prevents flame propagation back to the source of the process gas. Several instruments other instruments are designed to control electric catalytic oxidizer100. These instruments include one averaging pitot tube540, one flow indicator610, one differential pressure transmitter615, one pressure indicator620, one pressure switch625, one pressure alarm630and a sample port635. Averaging pitot tube540measures the total flow rate of the process gas. Differential pressure transmitter615converts the pressure signal from averaging pitot tube615to a milliamp signal. The milliamp signal may be used to determine the flow rate of the process gas. The signal may be fed into the control panel. In addition, the signal may be displayed on a chart recorder. The chart recorder displays the flow rate in standard cubic feet per minute and also records the flow rate.

Referring toFIG. 12, pressure switch625monitors the pressure of the process gas entering the oxidizing chamber. If the pressure is not above a preset minimum pressure, pressure switch625deactivates and sends a signal to the programmable logic controller in the control panel. The programmable logic controller then shuts down at least part of the process. Pressure gauge620indicates process gas pressure entering the oxidizing chamber. Some embodiments may also include a heat exchange550. Air to air heat exchanger550is adapted to pre heat the process gas entering the oxidizing chamber. Air to air heat exchanger550uses the hot process gas exiting catalyst570to heat the cool process gas entering the tube site of the air to air heat exchanger550.

As discussed above, electric heater560is designed to increase the temperature of the process gas, including the contaminated gas phase. Downstream of electric heater560are catalyst570and catalyst differential pressure switch650. The differential pressure switch650monitors the pressure drop across catalyst570. If the pressure drop increases to a pre set differential pressure the switch activates and sends a signal to the programmable logic controller. The programmable logic controller then shuts down at least part of the equipment.

Thermocouple660is located on the upstream side of catalyst570and measures the process gas temperature entering catalyst570. If the temperature at thermocouple660is too low, electric heater560is energized by the control panel. If the temperature at thermocouple660is too high, electric heater560is de-energized by the control panel. If the temperature at thermocouple660reaches a preset high temperature, a signal is sent to the programmable logic controller. The programmable logic controller then shuts down the equipment.

Thermocouple670is located on the downstream side of the catalyst570. Thermocouple670monitors the process gas temperature exiting catalyst570. If the temperature at thermocouple670reaches a preset temperature a signal is sent to the programmable logic controller. The programmable logic controller sends a signal to the oxidizer blower520to speedup. As oxidizer blower520speeds up, more dilution air is pushed into the oxidizing chamber which cools the temperature at thermocouple670. If the temperature at thermocouple670rises to a preset temperature a signal is sent to the programmable logic controller. The programmable logic controller then shuts down the equipment.

The gas which has been processed by the catalyst may exit the catalytic oxidizer100at exhaust stack580. In some embodiments, exhaust stack580is equipped with a sample port680, which is used to collect effluent gas samples. In some embodiments, exhaust stack580vents the hot process gas to atmosphere. In other embodiments, exhaust stack580recycles the processed gas to the water decontamination system.

Each catalytic oxidizer may have different conditions which produce the best result. These conditions likely depend on variables such as the type of catalyst, the flow rate, temperature, the particular contaminants, and the concentration of the contaminated gas.

One nonlimiting example of the electric catalytic oxidizer that can be used is the CCC SRCO 250E, available from Catalytic Combustion (Drewelow Remediation Equipment, Inc.). In this example, the contaminated gas phase which passes through the catalyst bed at a temperature of about 650° F. (343° C.).

Condenser System

One method of treating a contaminated gas phase includes condensing the gas phase contaminants. In some embodiments, the water decontamination system includes a condenser system. As discussed above, the condenser system may comprise a condenser that is air cooled or water cooled. In some embodiments, the condenser system comprises a condenser that is cooled by the contaminated water. In these embodiments, heat generated from the condensation of the contaminated gas phase may be exchanged with the contaminated water.

Referring toFIG. 13, the condenser system800may be equipped with one or more of a contaminated gas influent connection805, condenser810, contaminated liquid effluent connection815, clean air effluent connection820and clean air flow meter825. The process gas enters the condenser system800at influent connection805. As the contaminated gas phase passes through condenser810, at least some contaminants condense into concentrated liquid contaminants. The liquid contaminants may be removed from the condenser810at effluent connection815.

Ball valve830may be left open to continuously allow the condensed contaminants to be removed from the condenser system800. Alternatively, ball valve830may be closed to allow for the contaminants to collect in the condenser810. In some embodiments, cleaned air may be vented from the condenser810. This cleaned air may exit the condenser at cleaned air effluent connection820and be captured or vented to the atmosphere. Cleaned air may alternatively be recycled in one or more components of the liquid decontamination system. Such exit of the cleaned air may be monitored by cleaned air flow meter825.

Described above is one nonlimiting example of a condenser system. A person having ordinary skill in the art the skilled artisan will recognize the interchangeability of various features from different embodiments with the condenser system described and other available condenser systems.

A liquid decontamination system including at least one aerator module10, at least one separator tower200, and at least one condenser system800may be particular suited for applications which recover fuel and other volatile contaminants from water. Such fuel or other contaminants may then be recycled into various processes in which it was produced. For example, ships and other marine vehicles often collect bilge water. The bilge is the compartment at the bottom of the hull of a ship or other marine vessel where water collects so that it may be pumped out of the vessel at a later time. Bilge water often includes fuel and other volatile organic contaminants. By employing a liquid decontamination system, which includes a condenser system, the fuel and other volatile organic contaminants may 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 filter700which treats the contaminated gas phase. Suitable adsorption filter systems include, but are not limited to, activated carbon filtrations systems, zeolite filtration systems, and polymer filtration systems. Referring toFIG. 14, in some embodiments, the adsorption system700may receive a contaminated gas phase from the separator tower200. In some embodiments, the vacuum pump510delivers the contaminated gas phase to the adsorption system700. In some embodiments, the adsorption system700receives a contaminated gas phase from the aerator module10. In certain embodiments, the adsorption filtration system700receives more than one contaminated gas phase, including the contaminated gas phases from the aerator module10and the separator tower200.

In one embodiment, the adsorption filtration system700comprises an activated carbon filter that is suitable for removing contaminants from liquids. In some embodiments, the activated carbon filtration system is particularly suited for removing certain contaminants from water.

In some embodiments, the adsorption filtration system comprises one or more adsorption vessels705,710. In particular embodiments, these adsorption vessels705,710are activated carbon vessels. Such carbon vessels may be gas phase carbon vessels as gaseous contaminants are being purified in the vessel. In some embodiments, the gas phase contaminants may be first condensed and then purified through such adsorption vessels705,710.

The adsorption vessels may be selected based on the contaminant to be purified from the liquid and gas phase. Additionally, the vessels may be selected based on the desired flow rates of the overall process. In one example, an activated carbon vessel may 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, trichloroethylene, tetrachloroethylene, 1,1-dichloroethane, chloroform, 1,1,1-trichlorooethane, 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. One method of treating a contaminated gas phase from either the separator tower200or the aerator module10includes adsorbing the contaminants by activated carbon adsorption. In some embodiments, the liquid purification system comprises an activated carbon filtration system. The activated carbon filtration system may comprises one or more vapor phase carbon vessels, including, but not limited to two, three, four, and five carbon vessels. Contaminated gas phases are passed through the vapor phase carbon vessels.

Referring toFIG. 14, the adsorption filtration system700may include two purification vessels705,710, three sample ports715,720,725three manual ball valves730,735,740and an exhaust stack. The process gas passes through a pipeline741to the adsorption filtration system700. The process gas may enter the adsorption filtration system700through the process gas influent connection745. Averaging pitot tube750measures the total flow rate of the process gas being treated by the adsorption filtration system700. Temperature gauge755measures the temperature of the process gas being treated. Pressure gauge760measure the pressure of the process gas being treated. Sample port715is used to collect a process gas sample prior to treatment.

Adsorption vessels705,710may be used to treat the process gas. Such process gas enters adsorption vessels705,710through influent connections765,775. In the described embodiment, influent connections765,775is located near the bottom of adsorption vessels705,710. The process gas flows up through the adsorption medium706,711such as activated carbon, and the adsorption medium adsorbs the contaminants in the process gas. The process gas exits adsorption vessel705,710at the effluent connections770,780. In this embodiment, effluent connections770,780are located near the top of adsorption vessels705,710. Sample port720is used to collect a process gas sample after treatment by the primary adsorption vessel705. Ball valves730and735allow for servicing of primary adsorption vessel705.

Optionally, secondary adsorption vessel710may be used to further purify the contaminated gas phase that exits adsorption filter705. Ball valves735and740allows for servicing of secondary carbon vessel710. Downstream of effluent connection780is the exhaust stack751. The exhaust stack751may be equipped with a sample port725. The purified gas phase may then exit exhaust stack751to the environment or be recycled to the water decontamination system.

Examples of suitable activated carbon filters and vessels suitable for use in the liquid purification system include, but are not limited to, the MX-200-V available from Barnebey Sutcliffe, the AP3-60 and AP4-60 available from the Calgon Carbon Corporation. In some embodiments, the activated carbon may 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 the activated carbon may range from about 300 to about 600. In other embodiments, the density of the activated carbon may 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 no greater than 5 wt %.

Dual Phase

Water decontamination systems as described herein may also be used in a dual phase capacity. Often, a contaminated source of ground water will also include gaseous contaminants. Such contaminants may also be processed by the liquid decontamination systems and removed by the contaminated gas treatment system. In one embodiment, the gaseous contaminants are extracted from the ground or the soil and enter the aerator module. Such contaminants may pass directly to the headspace of the aerator tank and transferred to the contaminated gas treatment system. However, some embodiments may include a sensor which may recognize the gaseous contaminants which are being extracted from the ground or soil. Such sensor may then operate a valve that allows the gaseous contaminants to pass directly to the contaminated gas treatment system.

Mounting Configuration

The liquid decontamination system may be mounted one or more platforms. In one embodiment, each module of the water decontamination system is mounted on a separate skid. In such an embodiment, the user could choose the components and allocate each component to the desired location. However, in some embodiments, it is advantageous to mount all of the modules on one platform.

One example of a configuration is shown inFIGS. 15 and 16. In these figures, aerator tank101is mounted on a first skid67. Filtration module300, separator tower200, and contaminated gas treatment system201are mounted on a second skid68. Additionally, the second skid includes water transfer pump90, vacuum pump510, compressor20. As is noted in the Figures, separator tower module may include two separator towers200and203. Alternatively, separator tower203may be mounted on separator tower200. As is shown, separator tower203may be removed for ease of transportation of the skid68.

Manual or Automated Control

As is stated throughout the description, one or more processes and/or components may be controlled manually or automatically. Various valves, pressure gauges, temperature gauges, and pump controls allow a user to manually determine the conditions of operation of the water decontamination system. In some embodiments, it is preferable that these processes are controlled automatically. For example, one or more of the processes may be controlled from a control panel. In some embodiments, the control panel comprises one or more programmable logic controllers. Each controller may be designated certain processes to monitor, adjust, activate, or deactivate depending on preprogrammed settings and conditions. Modes of controlling these processes automatically will be understood by a person having ordinary skill in the art.

Unless otherwise indicated, the term “processing logic controller” is a broad term and is used in its ordinary sense and includes, without limitation, wherein the context permits, one or more steps, one or more groups, one or more programs, one or more instructions, and one or more processors. It may also refer to logic embodied in hardware or firmware, or to a collection of software instructions, possibly having entry and exit points, written in a programming language, such as, for example, C or C++. A processing module may be compiled and linked into an executable program, installed in a dynamic link library, or may be written in an interpreted programming language such as, for example, BASIC, Perl, or Python. It will be appreciated that processing modules may be callable from other modules (such as an input module) or from themselves, and/or may be invoked in response to detected events or interrupts. It will be further appreciated that processing modules may be comprised of connected logic units, such as gates and flip-flops, and/or may be comprised of programmable units, such as programmable gate arrays or processors.

Examples & Testing

Referring toFIG. 17, a liquid decontamination system was built and tested. This system included an aerator module10, a liquid transfer pump90, filtration system300, separator tower200, vacuum pump510, an electric catalytic oxidizer100. Additionally, a heat exchanger581was installed to transfer heat from liquid transfer pump90to the contaminated water prior to entering the separator tower200. All of these components are herein described.

Samples of contaminated water were tested. These samples contained various contaminants, such as VOCs. The samples were then purified using the liquid decontamination system. Samples were introduced at the liquid influent connection point on the aerator module10. Between samples, uncontaminated water was run through the liquid decontamination system for several hours.

The operation 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, separator tower vacuum pressure, separator tower temperature, and dilution air flow rate can be varied to adjust for certain contaminants and field conditions.

In some embodiments, the liquid purification system as described herein operates to produce about 10 gallons per minute of the purified liquid. However, the liquid purification system can be configured and/or scaled to produce more or less than 10 gallons per minutes, depending on the application and/or contaminants.

The samples were tested under the operation conditions described in Table 1.

The samples which were introduced to the liquid decontamination system were tested to determine the initial concentration of contaminants in the sample. This is referred to as the “Influent” concentration in the following tables. After introduction of the sample to the liquid decontamination system, further aliquots were taken at different points to determine the effectiveness of the various components of the liquid decontamination system. A “Midpoint” aliquots were taken immediately following the aeration tank to determine the efficiency of the aerator module10. “Effluent” aliquots were taken after the water was removed from the sump of the separator tower. In addition, Samples 4 & 6 presents data that describes the change in effectiveness of the contaminants based on the dilution air flow rate. Note that some of the data presented in the tables is given in terms of “<” (less than) some value because of the detection limits of the GC-MS testing device.

The following Tables 2-7 details the results of the testing:

According to the data, the liquid decontamination system substantially reduces the amount of contaminants in the contaminated water samples. Specific contaminants may be removed in greater amounts by varying the conditions of the liquid decontamination system. Furthermore, in all of the samples, cleaned exhaust was released to the environment in conformance with environmental regulations.

Other examples of water decontamination systems are described herein. Yet another example is the water decontamination system ofFIG. 18. In this embodiment, contaminated water passes through a first filtration system909. This prevents solid particles from entering aerator module10or any other component of the water decontamination system. The contaminated water then enters aeration module10and is decontaminated according to processes described above. As the water may not be at the selected temperature for decontamination, the water may pass through the aeration module10. In some embodiments, the system does not purify the water which is not at the selected temperature. In other embodiments, the water is decontaminated in the aerator module even at temperatures less than the selected temperature.

As water is transferred from the aeration module10by liquid transfer pump90, the water may be directed to filtration system300. Alternatively, if the water is not at a selected temperature, the water may be transferred and/or processed by heat exchanger911. This may be accomplished manually or automatically. For example, this may be accomplished by solenoid913which may automatically direct water to heat exchanger911. Heat exchange911exchanges heat from the vacuum pump with the contaminated water. In some embodiments, the contaminated water may then be transferred back to one or more components of the water decontamination system for further purification. For example, after passing through heat exchange911, the heated, contaminated water may pass back through filtration system300or back to aerator module10.

In another embodiment, the contaminated water may pass through heat exchanger921of the electric catalytic oxidizer100, or more generally, a heat exchanger921of the contaminated gas treatment system201. In one embodiment, and as illustrated inFIG. 14, the contaminated water may pass through heat exchanger911and heat exchange921, prior to passing back to one or more components of the liquid decontamination system, such as the aerator module10, the filtration system300, or the separator tower200. By allowing the water to pass through both heat exchangers, the water is heated more efficiently during the decontamination process.

After sufficient heating, solenoid valve913,914may redirect water to the aerator module or the filtration module. As water exits aeration module at or above the selected temperature ranger, the water may then flow through filtration system300and onto the separator tower200. The contaminated water may then be further purified by removal of the contaminants into a contaminated gas phase. This contaminated gas phase may then be further purified through a contaminated gas phase treatment system such as the electric catalytic oxidizer100.

The various methods and techniques described above provide a number of ways to carry out the invention. Of course, it is to be understood that not necessarily all objectives or advantages described may be achieved in accordance with any particular embodiment described herein.

Furthermore, the skilled artisan will recognize the interchangeability of various features from different embodiments. Similarly, the various features and steps discussed above, as well as other known equivalents for each such feature or step, can be mixed and matched by one of ordinary skill in this art to perform methods in accordance with principles described herein.

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 specifically disclosed embodiments to other alternative embodiments and/or uses and obvious modifications and equivalents thereof. Accordingly, the invention is not intended to be limited by the specific disclosures of preferred embodiments herein.