Fluid Processing System and Method

Abstract

To provide a fluid treatment system suitable for hardness reduction and contaminant removal.SOLUTION: A fluid treatment system and method may be operable to remove contaminants and optionally reduce hardness. The fluid treatment system may include a feed stream configured to provide contaminated fluid, a concentration tank configured to receive the contaminated fluid from the feed stream, a filtration unit configured to receive the contaminated fluid from the concentration tank, and a permeate stream operable to receive treated fluid from the filtration unit. The concentration tank may be operable to reduce the hardness of the contaminated fluid. The filtration unit may be operable to filter contaminants from the contaminated fluid.SELECTED DRAWING: Figure 1

Description

[Technical field]

[0001] CROSS-REFERENCE TO RELATED APPLICATIONS This application claims the benefit of and priority to U.S. patent application Ser. No. 14 / 070,263, filed Nov. 1, 2013, the entire contents of which are incorporated herein by reference.

[0002] The present disclosure, in some embodiments, relates to a fluid treatment system. More specifically, the present disclosure, in some embodiments, relates to a fluid treatment system suitable for hardness reduction and contaminant removal. [Background technology]

[0003] Fluids such as water can contain a variety of contaminants including, for example, dissolved organic carbon, metals, and metals that contribute to water hardness. Water hardness can refer to the presence of metals such as calcium or magnesium. Such metals and their corresponding ions can interfere with soap action, cause scale buildup, and further cause fouling of containment units or plumbing through electrochemical corrosion.

[0004] Contaminant removal and hardness reduction can be accomplished in a variety of ways, however, methods such as ion exchange, reverse osmosis and lime softening may require large equipment, large processing units, high chemical demands, and / or high cleaning demands. Summary of the Invention [Problem to be solved by the invention]

[0005] Thus, there is a need for improved fluid processing systems and methods that may allow for smaller equipment, smaller processing units, lower chemical requirements, and / or lower cleaning or purification requirements. [Means for solving the problem]

[0006] The present disclosure relates to a fluid treatment system, according to some embodiments. The fluid treatment system and method may be operable to remove contaminants and / or reduce hardness. The fluid treatment system may include a feed stream configured to provide a contaminated fluid, a thickening tank (e.g., a high solids contact reactor, etc.) configured to receive the contaminated fluid from the feed stream, a filtration unit configured to receive the contaminated fluid from the thickening tank, and an exit stream operable to receive a treated fluid from the filtration unit. The system may be operable to reduce hardness of the contaminated fluid (e.g., in the thickening tank). The filtration unit may be operable to filter contaminants from the contaminated fluid. The system may include, in some embodiments, a chemical inlet configured to admit coagulants, bases, and / or other chemicals to enable and / or facilitate metal oxidation, reduction, chemical precipitation, chemical coagulation treatments, or combinations thereof. The system may include the thickening tank and the filtration unit in a single adjacent integrated unit with synergistically enhanced performance.

[0007] In some embodiments, the filtration unit may include a ceramic membrane system. In some embodiments, reducing the hardness of the contaminated fluid may include precipitating metals from the contaminated fluid. The metals may include calcium and magnesium.

[0008] In some embodiments, the fluid treatment system may further include an aeration unit upstream of the concentrate tank. The aeration unit may be operable to remove CO2 content from the contaminated fluid. The aeration unit may include a dissolved oxygenator. The aeration unit or dissolved oxygenator may be operable to receive compressed air from a compressed air inlet. The compressed air inlet may be connected to the permeate side of the dissolved oxygenator. The aeration unit or dissolved oxygenator may include a substrate having pores less than 1 micron in diameter.

[0009] In some embodiments, the fluid treatment system may further include a chemical inlet upstream of the thickening tank. The chemical inlet may be configured to provide at least one coagulant to the contaminated fluid. The coagulant may promote coagulation of contaminants in the contaminated fluid. For example, the coagulant may remove turbidity and DOC. The at least one coagulant may be selected from alum (aluminum sulfate), ferric chloride or sulfate, polyaluminum chloride (PAC), and aluminochloro hydrate (ACH), and combinations thereof.

[0010] In some embodiments, the fluid treatment system may further include a pump. The pump may be disposed between the reactor (e.g., a thickening tank, etc.) and the filtration unit. The pump may be configured to regulate the flow of the contaminated fluid from the reactor to the filtration unit.

[0011] In some embodiments, the fluid processing system may further include a recirculation stream. The recirculation stream may be configured to receive the recirculation fluid from the filtration unit and to provide the recirculation fluid to the reactor. In some embodiments, the fluid processing system may further include a recirculation valve, which may be disposed on the recirculation stream and further configured to control the flow of the recirculation fluid from the filtration unit to the reactor. In some embodiments, the fluid processing system may further include a discharge stream, which may be disposed on the recirculation stream and further configured to discharge at least a portion of the recirculation fluid from the recirculation stream. In some embodiments, the fluid processing system may further include a discharge valve, which may be disposed on the discharge stream and further configured to control the flow of the discharge stream.

[0012] In some embodiments, the thickener tank may include 100 gallons per tank. The thickener tank may have at least one dimension that is generally circular having a diameter (e.g., 6 feet in diameter, etc.). The thickener tank may be configured and / or operated to have a retention rate of about 1 minute.

[0013] The present disclosure relates, according to some embodiments, to a method of fluid treatment, a method of hardness reduction and decontamination, and a method of operating a fluid treatment system. In some embodiments, the method may include providing a contaminated fluid from a feed stream, receiving the contaminated fluid in a thickener tank, receiving the contaminated fluid from the thickener tank in a filtration unit, and receiving a treated fluid from the filtration unit in a discharge stream. The thickener tank may be configured to reduce hardness of the contaminated fluid. The filtration unit may be configured to filter contaminants from the contaminated fluid.

[0014] In some embodiments, the filtration unit may include a ceramic membrane system. In some embodiments, reducing the hardness of the contaminated fluid may include precipitating metals from the contaminated fluid. The metals may include calcium and magnesium.

[0015] In some embodiments, the method includes an aeration unit upstream of the thickener tank. The aeration unit may be operable to remove CO2 content from the contaminated fluid using the aeration unit. The aeration unit may include a dissolved oxygenator. In some embodiments, the method may include receiving compressed air from a compressed air inlet at the dissolved oxygenator. The method may include connecting the compressed air inlet to a permeate side of the dissolved oxygenator.

[0016] In some embodiments, the dissolved oxygen addition device includes a substrate having holes with diameters of less than 1 micron. In some embodiments, the method may include passing compressed gas or compressed air through the substrate, forming sub-micron sized bubbles on a wetted side of the substrate, and scrubbing the sub-micron sized bubbles with a flow rate of about 4 1 / min sufficient to remove the bubbles before they expand.

[0017] In some embodiments, the method may include providing a chemical inlet upstream of the thickening tank and providing at least one coagulant and / or base to the contaminated fluid via the chemical inlet, the coagulant promoting coagulation of contaminants in the contaminated fluid. The at least one coagulant may be selected from the group including alum (aluminum sulfate), ferric chloride or ferric sulfate, polyaluminum chloride (PAC) and aluminum chlorohydrate (ACH), and combinations thereof.

[0018] In some embodiments, the method may include providing a pump between the concentrate tank and the filtration unit, and regulating a flow of the contaminated fluid from the concentrate tank to the filtration unit using the pump.

[0019] In some embodiments, the method may include providing a recirculation stream, receiving the recirculated fluid from the filtration unit in the recirculation stream, and providing the recirculated fluid in the recirculation stream to a concentrate tank. The method may include providing a recirculation valve on the recirculation stream and regulating a flow of the recirculated fluid from the filtration unit to the concentrate tank using the recirculation valve. The method may include providing a discharge stream on the recirculation stream and discharging at least a portion of the recirculated fluid from the recirculation stream via the discharge stream. The method may include providing a discharge valve on the discharge stream and regulating a flow of the discharge stream using the discharge valve.

[0020] Some embodiments of the present disclosure can be understood in part by reference to the disclosure and accompanying drawings. [Brief description of the drawings]

[0021] [Figure 1] 1 is a diagram of a fluid processing system in accordance with certain example embodiments of the present disclosure. [Diagram 2] 1 is a diagram of a fluid processing system in accordance with certain example embodiments of the present disclosure. [Diagram 3] 1 is a diagram of a fluid processing system in accordance with certain example embodiments of the present disclosure. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0022] Ion exchange water softening systems can simply replace calcium or magnesium (divalent cations) with sodium (Na-monovalent cation). A drawback of existing ion exchange (IX) technology is that IX resins can require frequent backwashing of salt (NaCl) or sodium hydroxide (NaOH) resulting in a waste brine solution, and IX raises the sodium concentration of the treated water in proportion to the hardness level. Because sodium has been associated with high blood pressure and heart disease, it can be desirable to avoid high sodium levels in water intended for human or animal use.

[0023] Reverse osmosis (RO) can be effective in filtering calcium and magnesium, but a key drawback can be hardness fouling (calcium easily blocks RO membranes). Therefore, RO membranes generally require chemical conditioning treatment and high cleaning requirements. Another key drawback is the large amount of brackish effluent produced (20%-25% of the stream) that requires further treatment or disposal.

[0024] Lime softening utilizes the addition of lime (Ca(OH)2) and sometimes soda ash to achieve the following reaction: (1)CO2+Ca(OH)2→CaCO3+H2O (2)Ca(HCO3)2+Ca(OH)2→2CaCO3+2H2O (3)Mg(HCO3)2+Ca(OH)2→CaCO3+MgCO3+2H2O Ca precipitates to CaCO3 and magnesium precipitates to MgCO3 via. Depending on the Ca and Mg levels, the pH after lime softening is 10.3 (for low Mg applications) to 11.0 (for high Mg applications). This means that after the hardness sludge is removed (e.g. via clarifiers or filtration methods), further chemical additions are required to neutralize the pH. Although CO2 does not accumulate in the hardness, it reacts quickly with lime, thus increasing the dosage required. These reactions are followed by settling and filtration.

[0025] Other types of water contaminants typically treated in drinking water include metals such as iron and manganese, as well as dissolved organic carbon (DOC). DOC results in TTHMs and HAAs after chlorination (secondary disinfection). Metal removal requires reaction tanks or vessels for chemical precipitation and / or oxidation to coagulate the metals so they can be removed via clarifiers and / or filters. Similarly, in coagulation processes, large tank or weir designs are required to allow the contaminants to coagulate into larger macro solids so they can be removed into clarifiers or filters. In both processes, there is a two-step process requiring two unit operations.

[0026] The present disclosure, in some embodiments, relates to articles, systems, and methods of use for fluid treatment systems. More specifically, the present disclosure, in some embodiments, relates to fluid treatment systems operable to remove contaminants from a contaminated fluid. The present disclosure, in some embodiments, relates to a method of decontaminating water, comprising forming contaminant solids in a reactor (e.g., a high solids catalytic reactor, etc.) and separating the contaminant solids from the water in a filter unit, which together provide a synergistic enhancement of contaminant removal. The forming of contaminant solids may include coagulation, precipitation, oxidation, reduction, or a combination thereof.

[0027] Some embodiments of the present disclosure may relate to a fluid treatment system for hardness reduction and / or contaminant removal. For example, the system may include a microfiltration or ultrafiltration unit configured to both precipitate hardness and filter precipitate. In some embodiments, the fluid treatment system may include a feed stream operable to provide a contaminated fluid. The contaminated fluid may include water or other fluids that may include dissolved organic carbon and other minerals or compounds that may form calcium, magnesium, multivalent cations, or any combination thereof.

[0028] In some embodiments, the separate reactor vessel upstream of the filter may be removed and / or eliminated. Without limiting any particular embodiment to a particular mechanism of action, the precipitation reactor may be eliminated because the hardness precipitation reaction occurs in the ceramic membrane system (e.g., CUF, etc.) and not in a separate reactor vessel upstream of the filter. In some embodiments, because CO2 is removed from the feedwater before reaching the filtration unit, and because the hardness precipitation reaction occurs inside the filtration unit, the accumulation of precipitated calcium carbonate and / or magnesium carbonate in the filtration system adjusts the pH in the filtration unit at a level that promotes the hardness precipitation reaction. In some embodiments, such a configuration (a) allows substantially all of the lime and / or soluble hydroxide ions added upstream of the filtration system to react directly with the hardness (e.g., not removed or used to raise the pH, meaning reduced chemical usage), and / or (b) allows the final pH of the softened water to be reduced by traditional lime softening approaches (e.g., due to reduced process chemical additions). Post neutralization may not be required.

[0029] feed stream In some embodiments, the supply stream may include a pipe or tube. The pipe or tube may include a particular material and may further have a particular length or diameter. The supply stream may have a particular flow rate or flow rate of the contaminated fluid therein. The particular material, size and specifications of the pipe, such as length and diameter, and the flow rate may be varied without departing from the description herein.

[0030] Aeration Unit In some embodiments, the fluid treatment system may further include an aeration unit. The aeration unit may be located upstream of the thickening tank. The aeration unit may be in fluid communication with the feed stream. The fluid connection may be established via coupling or otherwise appropriately connecting the aeration unit to the feed stream. The aeration unit may be located along the feed stream, configured to receive the contaminated fluid therein, and further configured to provide the contaminated fluid therein to the thickening tank. Various aeration units may be used without departing from the description herein. In some embodiments, the aeration unit may include a dissolved oxygen (DO) dosing device.

[0031] The aeration device can advantageously allow contaminants in the contaminated fluid to be oxidized. In some embodiments, the aeration device can advantageously allow metals in the contaminated fluid to be oxidized. The aeration unit may include a compressed air inlet configured to provide compressed air to the contaminated fluid. The compressed air inlet can allow the compressed air to contact the contaminated fluid in a steady, metered amount. The addition of compressed air can allow CO2 to be removed from the contaminated fluid. In some fluid treatment systems, CO2 can react with the hydroxide-based precipitant or coagulant before the hardness reacts with the precipitant or coagulant. CO2 reacting with the precipitant or coagulant can thus prevent the hardness from reacting with the precipitant or coagulant. CO2 reacting with the precipitant can increase the dosage of the hydroxide-based precipitant and also unnecessarily raise the pH of the contaminated fluid. Thus, removing the CO2 content prior to introducing a precipitant or coagulant into a fluid treatment system can advantageously allow for a faster reaction rate between the hardness and the precipitant or coagulant. Removing the CO2 content can also advantageously control the pH of the contaminated fluid within the fluid treatment system.

[0032] In some embodiments, the aeration unit may include a DO adder. The DO adder can oxidize metals (such as iron) to create insoluble metal oxides. With the DO adder, the system can oxidize metals and also remove hardness in one unit operation. In some embodiments, the aeration unit can advantageously reduce the chemical requirements for achieving a desired level of hardness reduction by removing dissolved CO2 prior to the addition of hydroxide precipitants. In some embodiments, the aeration unit may not be necessary for a desired level of hardness reduction or contaminant removal. In some embodiments, the aeration unit can advantageously reduce the operating costs of the fluid treatment system.

[0033] In some embodiments, metals may be removed from the contaminated fluid by oxidizing the metals to insoluble metal oxides. The compressed gas inlet may be coupled, connected, or otherwise in communication with a compressed gas source. The compressed gas source and compressed gas inlet may be operable to provide compressed gas, and may further provide, for example, compressed air or oxygen. Gas flow in the compressed gas inlet may be controlled by a valve or a mass flow controller or other control device.

[0034] In some embodiments, a cross-flow filtration device can be used, and a compressed gas source can be connected to the permeate side (dry side) of the DO addition device. The compressed gas can have a pressure greater than the pressure of the contaminated fluid. Thus, when the compressed gas is introduced into the DO addition device, the compressed gas can push through the DO addition device, or more specifically, the substrate of the device. When the compressed gas pushes through the substrate of the DO addition device, bubbles can form in the liquid medium.

[0035] If both metal removal and hardness removal are desired or required, the aeration system can facilitate both in some embodiments. The aeration system can reduce the chemical requirements for hardness removal by oxidizing metals to insoluble metal oxides and removing CO prior to the addition of hydroxide-based precipitants.

[0036] In some fluid processing systems, large bubbles may form when compressed gas is passed over a substrate. The large bubbles may have sufficient buoyancy to lift off the substrate. Thus, the large bubbles may float to the top surface of the contaminated liquid medium or fluid. The floating of the bubbles to the top surface may facilitate air stripping of contaminants present in the contaminated fluid.

[0037] According to an embodiment of the present disclosure, passing or passing compressed gas through small holes or pores in the substrate of the DO addition apparatus may generate bubbles on the side of the substrate through which the fluid passes. The generated bubbles may be micro bubbles or may be sub-micron in size. Sub-micron sized bubbles may have significantly less buoyancy than larger bubbles. Thus, the generated bubbles may be small enough that their buoyancy does not allow them to overcome the surface tension of the substrate. Thus, the generated bubbles may not leave the substrate and may not even rise above the contaminated fluid. Instead, the generated bubbles may remain substantially attached to or in close proximity to the surface of the substrate. In some embodiments, only washing of the contaminated fluid passing along the wet side of the substrate in the DO addition apparatus may cause bubbles to be released into the contaminated fluid.

[0038] According to an embodiment of the present disclosure, generating sub-micron sized bubbles can substantially increase the contact surface of oxygen in the DO addition device. Smaller bubbles can provide a larger surface area to volume ratio using the same amount or volume of gas compared to larger bubbles. Thus, by utilizing the disclosed principles, the surface area to volume ratio of air or oxygen gas introduced into the DO addition device can be maximized. In other words, a greater number of smaller bubbles can be generated than larger bubbles using the same volume of gas. Thus, by generating smaller bubbles, the surface area of ​​oxygen in the contaminated fluid can be increased. In turn, the contact of oxygen with the contaminated fluid can be significantly increased without significantly increasing the volume of gas introduced.

[0039] In some embodiments, a ratio of about 76 l / min of contaminated fluid per 30 l / min of pressurized gas can be achieved. In some embodiments, pressurized pure oxygen can be used. In embodiments where pressurized pure oxygen is used, a ratio of about 76 l / min of contaminated media per nominally 6 l / min of pressurized oxygen can be achieved. According to the present disclosure, any type of filter unit can be used in place of the DO dosing device without departing from the description herein. A suitable filter may be operable to produce bubbles as defined herein and to oxidize metal particles in the liquid medium passing therethrough.

[0040] In some embodiments, the increased pressure of the compressed gas, together with the hydrodynamics of the gas passing through the holes in the substrate and being washed by passing the fluid, can result in highly turbulent mixing action within the DO addition device. In some embodiments, high Reynolds numbers in the turbulent range can be effective. High Reynolds numbers can be achieved using a contaminated fluid flow rate of about 4 l / min through a 4 mm channel. The contaminated fluid can be discharged into the permeate side of a cross-flow filtration unit that utilizes a ceramic membrane with openings that can be less than 1 micron in diameter.

[0041] The net effect of high turbulent mixing and maximized surface area to volume ratio of the introduced gas may be that significantly less volume of gas is required and the contaminated fluid can be saturated with dissolved oxygen. Furthermore, the buoyancy of the bubbles can keep them from leaving the substrate and therefore from entering or rising to the top of the fluid flow, so that the bubbles can only be removed by the passing liquid medium that washes the wetted side of the substrate. In some embodiments, the oxygen provided by the bubbles can be more evenly diffused through the contaminated fluid or liquid medium. Thus, the efficiency of the fluid treatment process and the oxidation process can be increased.

[0042] In some embodiments, the contaminated fluid leaving the DO addition device may include insoluble metal particles. Insoluble metal particles may tend to flocculate into relatively large particles. In some embodiments, larger particles such as insoluble metal particles may settle to the bottom of a settling tank. In some embodiments, larger particles such as insoluble metal particles may be removed using any type of filtration system. Such methods of filtering insoluble metal particles may advantageously reduce or eliminate the need for aggressive chemicals. Other advantages may include reducing or eliminating the need to discharge compounds into a sewer system or dispose of chemicals at an off-side treatment facility. Additionally, costs associated with such actions may also be reduced or eliminated.

[0043] Coagulant In some embodiments, the fluid treatment system may further include a chemical inlet. The chemical inlet may be located downstream of the aeration unit and / or upstream of the high solids contactor reactor. The chemical inlet may be located upstream of the thickening tank and / or may be operable to meter a selected coagulant or precipitant into the contaminated fluid. The coagulant may include one or more metal salts in some embodiments. The coagulant may destabilize the charge on the (e.g., solid and dissolved) molecules, coagulating the contaminants together into solids. Once the contaminants are coagulated, they may be filtered. Contaminants that may be removed using the coagulant may include, for example, dissolved organic carbon (DOC), color-imparting contaminants such as ligands, and turbidity.

[0044] Coagulation typically occurs in large dedicated reaction vessels, however some embodiments of the present disclosure differ in that coagulation is facilitated in thickener tanks via high solids mixing, making a separate coagulation tank unnecessary.

[0045] The coagulant may be selected based on the composition or other characteristics of the contaminated fluid. In some embodiments, the use of more than one coagulant may be desirable. Suitable coagulants may include alum (aluminum sulfate), ferric chloride or sulfate, polyaluminum chloride (PAC) and aluminum chlorohydrate (ACH), and combinations thereof. Other coagulants may be selected as needed to target specific contaminants within the contaminated fluid. Similarly, combinations of coagulants, in the same or different proportions, may be selected to achieve a desired coagulation effect. The coagulant provided by the chemical inlet may be operable to promote and / or facilitate removal of dissolved organic compounds.

[0046] Hydroxide Precipitants In some embodiments, the fluid treatment method may include the addition of Ca(OH)2 or lime. Lime addition may be accomplished by direct addition of Ca(OH)2. In some embodiments, Ca(OH)2 may be introduced indirectly by the addition of a soluble hydroxide compound. The soluble hydroxide compound may include sodium hydroxide NaOH and / or potassium hydroxide KOH. The indirect addition of lime is accomplished by the addition of Ca(OH)2, which has the following chemical formula: 2OH - +Ca(HCO3)2→2HCO3 - +Ca(OH)2.

[0047] Whether the Ca(OH)2 is added directly or indirectly, the addition can facilitate precipitation removal of hardness in the contaminated fluid. Ca(OH)2-enhanced precipitation removal of hardness can occur in a thickener tank according to the present disclosure. Hardness precipitation removal can include precipitation of calcium and magnesium into carbonates. The precipitated carbonates can build up in a thickener loop of a fluid treatment system according to the present disclosure.

[0048] Concentration Tank In some embodiments, the fluid treatment system may further include a concentrate tank. The concentrate tank may be in fluid communication with the feed stream. Thus, the feed stream containing the contaminated fluid may be operable to provide the contaminated fluid to the concentrate tank, and the concentrate tank may be further operable to receive the contaminated fluid from the feed stream. In some embodiments, an aeration unit and / or a chemical inlet may be located upstream of the concentrate tank. In some embodiments, the concentrate tank may be in fluid communication with the aeration unit and / or the chemical inlet. Thus, the concentrate tank may receive the contaminated fluid downstream of the aeration unit and / or the chemical inlet.

[0049] The thickening tank may have any desired size, shape, and orientation in some embodiments. For example, the thickening tank may be generally cylindrical and may be generally vertically oriented. In some embodiments, the thickening tank may include a reactor. The bulk and size of the thickening tank may vary to achieve various functional needs. In some embodiments, a larger thickening tank may be operable to receive a larger volume of contaminated fluid. In some embodiments, a smaller thickening tank may be more cost-effective. In some embodiments, the thickening tank may include a volume of about 800 gallons. In some embodiments, the thickening tank may include a diameter of about 6 feet. Different reactor designs or types may be selected depending on factors such as the characteristics or concentration of contaminants in the feed stream.

[0050] In some embodiments, the thickening tank may utilize cross-flow filtration or may exhibit a cross-flow mechanism. In some embodiments, the thickening tank may exhibit a residence time of about 30 seconds to about 5 minutes depending on the application. According to some embodiments, the high flow rate from the cross-flow filtration associated with a relatively high concentration of precipitated and / or coagulated and / or oxidized contaminants creates a high solids contact reactor in the ultrafiltration device. This can promote and / or accelerate the reaction in the thickening tank. The process may function (e.g., may function well) if accumulated solids are present in the tank (to promote further reaction). A blowdown (e.g., intermittent, continuous) may be performed to release some solids that accumulate in the system. If performed, at least some solids are allowed to remain in the system (e.g., in the tank, etc.). The amount of solids to be retained after the blowdown can be selected (e.g., empirically) to be sufficient to nucleate further precipitation reactions at a desired rate.

[0051] In some embodiments, the thickener tank may be operable to reduce hardness of the contaminated fluid. Water or fluid hardness may arise when the water or fluid has high calcium and / or magnesium content. The thickener tank may reduce hardness by removing multivalent cations that may arise from mineral content. In some embodiments, the thickener tank may reduce hardness by precipitating hardness from the water or fluid or precipitating multivalent cations from the water or fluid. Precipitating hardness may include precipitating calcium and magnesium into carbonates. The precipitated carbonates may be deposited in a concentrate loop of a fluid treatment system according to the present disclosure. In some embodiments, providing the right chemistry and / or mix may be the key variable in precipitating calcium and magnesium.

[0052] pump In some embodiments, the fluid treatment system may further include a pump. The pump may be disposed between the concentrate tank and the filtration unit. The pump may be in fluid communication with a discharge flow of the concentrate tank. The pump may be configured to regulate a flow rate of concentrated fluid from the concentrate tank to the filtration unit to generate a desired cross-flow through the filtration unit and to provide sufficient mixing in the concentrate tank.

[0053] Various types of pumps may be used without departing from the description herein, in some embodiments, the pump may be a centrifugal pump, a horizontal pump, or a screw pump.

[0054] Filtration Unit In some embodiments, the fluid treatment system may further include a filtration unit. The filtration unit may be in fluid communication with a concentrate tank. Thus, the filtration unit may be operable to receive concentrated fluid from the concentrate tank, and the concentrate tank may be operable to provide concentrated fluid to the filtration unit. A pipe or tube may be used to establish fluid communication between the concentrate tank and the filtration unit. The pipe or tube for establishing fluid communication may include a specific material and may have a specific length or diameter. The size and material used may vary without departing from the description herein. In some embodiments, the size of the pipe may depend on the desired cross-flow flow rate for the ceramic membrane. The cross-flow flow rate may range from 1 to 10 times the permeate flow rate (e.g., depending on the material being filtered).

[0055] In some embodiments, the filtration unit may be operable to filter contaminants from the contaminated fluid. The contaminants from the contaminated fluid may include total suspended solids (TSS), pathogens, oxidized contaminants, coagulated contaminants, and precipitated contaminants. In some embodiments, the contaminants in the water or fluid may include precipitates of multivalent cations that may contribute to hardness.

[0056] In some embodiments, the filtration unit may include a ceramic membrane filtration unit. In some embodiments, the ceramic membrane filtration unit may include an ultrafiltration membrane, a nanofiltration membrane, or a microfiltration membrane. Different membranes or types of ceramic membrane filtration units may be selected depending on the contaminants in the contaminated fluid. In some embodiments, the ceramic membrane filtration unit may include a pore size of 1 nm to 900 nm. In some embodiments, the ceramic membrane filtration unit may include materials such as α-Al2O3, γ-Al2O3, TiO2, ZrO2, or SiO2. Other materials may be used without departing from the description herein.

[0057] The filtration unit may be configured to operate as a cross-flow filter in some embodiments. The cross-flow action may provide shear at the membrane wall, which may contribute to reduced cleaning and / or fouling of the membrane. The filtration unit may, for example, include a body having at least one channel extending therethrough. The channel may include an inlet configured to admit fluid into the filtration unit, an outlet in fluid communication with the inlet and configured to allow a flow-through fluid (e.g., concentrated media) to exit the filtration unit, and a membrane. At least a portion of the channel may be defined by a membrane, the membrane having a fouled media surface in fluid communication with the inlet and outlet, and an opposing permeate surface. The filtration unit may further include a second outlet in fluid communication with the permeate surface and configured to allow a treated fluid media (permeate) to exit the filtration unit. The filtration may include a first portion in fluid communication with the inlet and outlet, and a second portion in fluid communication with the permeate outlet. Fluid communication between the first and second portions may be mediated by a membrane interposed between the two. The first portion may otherwise be sealed from the second portion to reduce or prevent membrane bypass. The filtration unit may have any desired size, shape, or orientation. For example, the filtration unit may be generally cylindrical and may be generally horizontally oriented. The inlet may be located at one end and the concentrate outlet may be located at the opposite end. The permeate outlet may be located anywhere, including, for example, extending from the side of the unit at or near its center.

[0058] permeate flow In some embodiments, the fluid treatment system may further include a permeate operable to receive the treated fluid from the filtration unit. The treated fluid may be a fluid that may have reduced hardness and may have contaminants removed. The treated fluid may be or may include the permeate from the filtration unit. The permeate may include a pipe or tube in fluid communication with the filtration unit. The pipe or tube may include a particular material and may have a particular length or diameter as desired. The feed stream may have a particular flow rate or flow rate of the contaminated fluid therein. The particular material, size and specifications, such as length and diameter, of the pipe, and the flow rate may be varied without departing from the description herein.

[0059] Recirculation Loop In some embodiments, the fluid processing system may further include a recirculation loop or a recirculation stream. The recirculation stream may be configured to receive fluid from the filtration unit and to provide fluid to the concentrate tank. In some embodiments, the fluid provided to the concentrate tank by the recirculation stream may include at least a portion of the fluid from the filtration unit. In some embodiments, the inlet of the recirculation loop and / or the feed stream may be in fluid communication generally with an upper portion of the concentrate tank and / or may be in fluid communication generally opposite an outlet of the concentrate tank (e.g., an outlet in fluid communication with the filtration unit).

[0060] Recirculation Valve In some embodiments, the fluid processing system may further include a recirculation valve. The recirculation valve may be disposed on the recirculation flow and / or may be configured to provide a pressure (e.g., a specified or desired pressure, etc.) and / or a cross-flow flow rate within the filtration unit. Various types of valves may be used without departing from the description herein. In some embodiments, the recirculation valve may be a ball valve, a butterfly valve, a plug valve, a needle valve, a pinch valve, a gate valve, an annular valve, a diaphragm valve, or other suitable valve.

[0061] discharge stream In some embodiments, the fluid treatment system may further include a discharge stream. The discharge stream may be disposed on the recirculation stream and / or may be configured to allow removal of at least a portion of the solids from the system. The discharge stream may be configured to receive at least a portion of the fluid in the recirculation stream. The received fluid may include a substantial concentration of precipitated hardness and / or contaminants removed from the contaminated fluid provided by the feed stream.

[0062] The exhaust stream may include a pipe or tube in fluid communication with the recirculation stream. The pipe or tube may include a particular material and may further have a particular length or diameter. The supply stream may have a particular flow rate or flow rate of the contaminated fluid therein. The particular material, size and specifications of the pipe, such as length and diameter, and flow rate may be varied without departing from the description herein.

[0063] Exhaust valve In some embodiments, the fluid treatment system may further include an exhaust valve. The exhaust valve may be disposed on the exhaust stream. The exhaust valve may be configured to control the flow of fluid from the recirculation stream through the exhaust stream. In some embodiments, the exhaust valve may stop and / or start the flow of contaminated fluid therethrough. Various types of valves may be used without departing from the description herein. In some embodiments, the exhaust valve may be a ball valve, a butterfly valve, a plug valve, a needle valve, a pinch valve, a gate valve, an annular valve, a diaphragm valve, or other suitable valve.

[0064] Additional components In some embodiments, additional items such as pumps or valves may be used without departing from the description herein. For example, in some embodiments, additional pumps, such as centrifugal pumps, horizontal pumps, screw pumps, and other pumps, may be added as part of the fluid processing system to regulate the flow of various fluid streams therein. As another example, in some embodiments, additional valves, such as ball valves, butterfly valves, plug valves, needle valves, pinch valves, gate valves, annular valves, diaphragm valves, or other suitable valves, may be added as part of the fluid processing system to control or regulate the flow of various fluid streams therein.

[0065] pH control In some embodiments, the fluid treatment systems of the present disclosure can advantageously control the variation in pH of the contaminated fluid during hardness reduction and contaminant removal processes. In some fluid treatment systems, precipitating calcium and magnesium into calcium and magnesium carbonates can raise the pH level of the resulting fluid stream. In some systems, the pH level may increase as high as 10 or even more. For some purposes, an increase in pH level may be undesirable.

[0066] In some fluid treatment systems, a pH neutralizing agent may be added or may be necessary to reduce or control the increase in pH level of the fluid. In some embodiments of the present disclosure, the configuration of the aeration unit, chemical inlet, and thickener tank may control the pH level such that a later neutralizing agent may not be required for the fluid treatment process or system. The aeration unit may be operable to remove CO2 from the feed stream before hardness reduction occurs. As a result, in some embodiments, essentially all of the lime and / or soluble hydroxide ions added upstream may react directly with the hardness. Only a near stoichiometric addition of hydroxide chemicals may be required in some embodiments. Because the precipitation reaction occurs in the thickener tank, where high concentrations of CaC03 and / or MgC03 are present, hydroxide chemicals are not required to raise the pH above 10. CaC03 and / or MgC03 in the thickener tank promotes dissolved Ca and Mg precipitation at pH levels below 9. Thus, the pH of the treated water may be less than 9 in some embodiments.

[0067] Control of pH can, in some embodiments, allow desirable reactions to be enhanced. For example, raising the pH upstream can enhance reactions within the vessel. If the pH is, for example, below 7, a base can be added. In some embodiments, by increasing the pH (e.g., from below 7 to above 7), metal and / or hardness removal can be enhanced.

[0068] In some embodiments of the present disclosure, the fluid treatment system and method can advantageously reduce the need for subsequent neutralizing agents, thereby advantageously reducing the chemical footprint and chemical demands. In some embodiments of the present disclosure, the treated fluid can have a pH of about 9 or less.

[0069] Enhanced mass transfer In some embodiments, the fluid treatment system may utilize cross-flow filtration or may exhibit a cross-flow mechanism. In cross-flow filtration, the incoming feed stream may pass through the surface of a cross-flow membrane. In some cross-flow filtration systems, two outlet streams may be generated. The permeate stream may be a portion of the fluid that passes through the membrane. The permeate stream may contain some soluble and / or insoluble components from the feed stream or contaminated fluid. The components in the permeate stream may be smaller than the removal rating or pore size of the membrane. The concentrate stream may be the remainder of the feed stream or contaminated fluid that did not pass through the membrane.

[0070] In some embodiments, cross-flow filtration and cross-flow mechanisms can improve mass transfer and promote intermixing of fluids. Enhanced mass transfer can promote component contact, where more contact between different components occurs. Component contact can result in a desired reaction. Thus, enhanced materials can allow for faster reaction rates, such as faster precipitation rates for hardness reduction.

[0071] In some embodiments, the cross-flow filtration utilized by the fluid treatment system may advantageously provide a sink-like effect. Solids present in the contaminated fluid entering the thickener tank may act as a sink, further attracting contaminants as they enter the thickener tank. The sink-like effect may synergistically facilitate further hardness reduction and contaminant removal.

[0072] Honing Materials In some fluid treatment systems, a honing material can be added to the fluid. The honing material can advantageously clean contaminants from the filtration membrane. Thus, the fluid treatment system can add the honing material to prevent fouling of the filtration membrane.

[0073] In some embodiments of the present disclosure, precipitated calcium carbonate, magnesium carbonate, or other metal precipitates can demonstrate the same effect as honing materials. In some embodiments, precipitated calcium carbonate or magnesium carbonate can help clean contaminants from filtration membranes. Thus, in some embodiments, a separate honing material may not need to be added to the fluid treatment system. The ability of precipitated calcium carbonate or magnesium carbonate to act as a honing material can advantageously reduce membrane cleaning requirements, such as the need for a separate honing material. The ability of precipitated calcium carbonate or magnesium carbonate to act as a honing material can also advantageously reduce operating costs.

[0074] Small size / miniaturization In some embodiments of the present disclosure, the fluid treatment system may be substantially more compact or space efficient than conventional hardness removal systems. In some embodiments, the concentrate tank of the fluid treatment system may include a volume of about 800 gallons. In some embodiments, the concentrate tank of the fluid treatment system may include a diameter of about 6 feet. In some embodiments, the more compact and space efficient fluid treatment system may be more cost effective.

[0075] In some embodiments, the fluid treatment systems of the present disclosure may eliminate the need for a precipitation reactor or a separate filtration tank or system.

[0076] In some embodiments, the fluid treatment systems of the present disclosure can reduce chemical footprints and chemical demands, hi some embodiments, increased mass transfer in the fluid treatment systems of the present disclosure can allow for shorter treatment or residence times.

[0077] How to use In some embodiments, the present disclosure relates to a method for treating a fluid or operating a fluid treatment system, and more particularly, in some embodiments, the present disclosure relates to a method for fluid hardness reduction and decontamination.

[0078] In some embodiments, a method of fluid treatment may include providing a feed stream including the contaminated fluid to a concentrate tank. The method may further include receiving the contaminated fluid in the concentrate tank. The method may further include reducing the hardness of the contaminated fluid in the concentrate tank. A concentrate tank according to embodiments of the disclosed method may be configured to reduce the hardness of the contaminated fluid. In some embodiments, reducing the hardness of the contaminated fluid may include precipitating metals from the contaminated fluid. Metals precipitated from the contaminated fluid may include calcium, magnesium, and other metals that may be oxidized.

[0079] The method of fluid treatment may include (e.g., may further include) transferring the concentrated fluid from the concentrate tank to a filtration unit. The method of fluid treatment may include (e.g., may further include) receiving the concentrated fluid from the concentrate tank at a filtration unit. A filtration unit according to embodiments of the disclosed method may be configured to filter contaminants from the concentrated fluid. In some embodiments, the filtration unit may be a ceramic membrane system or a ceramic membrane filtration unit. The method may further include transferring the treated fluid from the filtration unit. The treated fluid may be received from the filtration unit in a discharge stream.

[0080] In some embodiments, an aeration unit can be located upstream of the concentration tank. The aeration unit may include a DO addition device. A compressed air inlet or compressed gas inlet may be coupled to the DO addition device. In some embodiments, the method according to the present disclosure may further include receiving compressed air from the compressed air inlet at or through the DO addition device. In some embodiments, the method may further include removing CO2 content from the contaminated fluid using the aeration unit.

[0081] In some embodiments, the compressed gas inlet or compressed air inlet can be connected to the permeate side of the DO addition device. The DO addition device can include a substrate, and the substrate can include holes of a specific diameter. The holes in the substrate can have a diameter of less than 1 micron. The compressed gas provided by the compressed gas inlet can be passed through the substrate. The compressed gas passed through the substrate can form sub-micron sized bubbles on the wetted side of the substrate. The generated bubbles can be small enough that their buoyancy does not allow the bubbles to overcome the surface tension of the substrate. Thus, the generated bubbles can remain attached to the side of the substrate and do not rise to the top of the contaminated fluid. The generated sub-micron sized bubbles can then be washed at a flow rate of about 4 l / min.

[0082] In some embodiments, the method may further include providing a chemical inlet upstream of the thickening tank. At least one coagulant and / or base may be provided to the contaminated fluid via the chemical inlet. The coagulant may be selected from the group including alum (aluminum sulfate), ferric chloride or ferric sulfate, polyaluminum chloride (PAC) and aluminum chlorohydrate (ACH), and combinations thereof. Other coagulants may be chosen depending on the contents or characteristics of the contaminated fluid. The coagulant introduced into the contaminated fluid may promote the coagulation of contaminants in the contaminated fluid.

[0083] In some embodiments, the method may further include providing a pump between the concentrate tank and the filtration unit, the pump being operable to regulate the flow of concentrated fluid from the concentrate tank to the filtration unit.

[0084] In some embodiments, the method may further include providing a recirculation stream. The method may include receiving the recirculation fluid from the filtration unit in the recirculation stream. The method may include providing the recirculation fluid in the recirculation stream to a thickening tank.

[0085] In some embodiments, the method may further include providing a recirculation valve on the recirculation stream and / or actuating the recirculation valve on the recirculation stream. The recirculation valve may be operable to regulate a flow of the recirculation fluid from the filtration unit to the thickening tank using the recirculation valve. In some embodiments, the method may further include providing a drain stream on the recirculation stream. At least a portion of the recirculation fluid may be drained via the drain stream. In some embodiments, the method may further include providing a drain valve on the drain stream. The drain valve may be operable to regulate a flow of the drain stream.

[0086] Specific Example Embodiments A particular example embodiment of a fluid treatment system is illustrated in Figure 1. Figure 1 illustrates a fluid treatment system 100 that may be operable to treat a contaminated fluid 101. More specifically, the fluid treatment system 100 may be configured for hardness reduction and contaminant removal. As seen in Figure 1, the fluid treatment system 100 may include a feed stream 103. The feed stream 103 may be operable to provide the contaminated fluid 101 therein.

[0087] The feed stream 103 may be in fluid communication with an aeration unit 105. The aeration unit 105 may be operable to remove CO2 content from the contaminated fluid. In some embodiments, the aeration unit 105 may be a DO addition device. In some embodiments, the aeration unit 105 may be coupled or otherwise connected to a compressed gas inlet 107. The compressed gas inlet 107 may be operable to provide a flow of compressed gas or compressed air into the aeration unit 105 or the DO addition device. The aeration unit 105 may include a substrate (not shown) therein. The compressed gas inlet may be coupled or otherwise connected to the aeration unit 105 on the permeate side of the aeration unit 105.

[0088] In some embodiments, a chemical inlet 109 may be disposed downstream of the aeration unit 105. The chemical inlet 109 may be coupled to or in fluid communication with the output fluid stream of the aeration unit 105. The chemical inlet 109 may be configured to provide at least one coagulant, base, or other material to the contaminated fluid 101. The at least one base may be selected from a group including calcium hydroxide, sodium hydroxide, and potassium hydroxide. The coagulant may be selected from alum (aluminum sulfate), ferric chloride or sulfate, polyaluminum chloride (PAC), and aluminum chlorohydrate (ACH), and combinations thereof.

[0089] A concentration reactor 110 may be disposed downstream of the aeration unit 105 and downstream of the chemical inlet 109. The concentration reactor 110 may be operable to receive the contaminated fluid 101. The concentration reactor 110 may be operable to reduce the hardness of the contaminated fluid 101. The concentration reactor 110 may include 800 gallons / tank and may further include a 6 foot diameter. The concentration reactor 110 may have a retention rate of about 1 minute.

[0090] The concentration reactor 110 may be in fluid communication with the filtration unit 120. A pump 116 may be provided therebetween. The pump 116 may be configured to drive and / or regulate the flow of the concentrated fluid 113 from the concentration reactor 110 to the filtration unit 120.

[0091] In some embodiments, a filtration unit 120 can be provided downstream of the concentration reactor 110 and further downstream of the pump 116. The filtration unit 120 can be operable to filter contaminants from the concentrated fluid 113. In some embodiments, the filtration unit 120 can be a ceramic membrane system.

[0092] In some embodiments, the discharge stream 121 may be coupled or otherwise connected to a filtration unit 120. The discharge stream 121 may include a treated fluid 123 from the filtration unit 120.

[0093] Fluid treatment system 100, in some embodiments, may recirculate fluid 125 from filtration unit 120 back to concentration reactor 110. The recirculation fluid 125 may be recirculated via a recirculation stream 127. The recirculation stream 127 may be configured to receive the recirculation fluid 125 from the filtration unit 120 and to provide the recirculation fluid 125 to the concentration reactor 110. In some embodiments, a recirculation valve 142 may be disposed on the recirculation stream 127 and further configured to control the flow of the recirculation fluid 125 from the filtration unit 120 to the concentration reactor 110.

[0094] In some embodiments, the fluid treatment system 100 may include a discharge stream 131 disposed on the recirculation stream 127. The discharge stream 131 may be configured to discharge at least a portion of the recirculation fluid 125 from the recirculation stream 127. A discharge valve 130 may be disposed on the discharge stream 131 and may be further configured to control the flow of the discharge stream 131.

[0095] A particular example embodiment of a fluid treatment system is illustrated in Figure 2. Figure 2 illustrates a fluid treatment system 200 that may be operable to treat a contaminated fluid 201. System 200 includes an inlet 202, a high solids catalytic reactor 210, a pump 216, a filtration unit 220, a discharge stream 222, and a recycle stream 240. Fluid treatment system 200 may be configured for contaminant removal. As seen in Figure 2, fluid treatment system 200 may include a feed stream 203. Feed stream 203 may contain contaminated fluid 201 therein.

[0096] The concentration reactor 210, in some embodiments, may be located downstream of the chemical inlet 209. The concentration reactor 210 may include an opening 212 that may be open to the atmosphere. The concentration reactor 210 may be operable to receive the contaminated fluid 201. The concentration reactor 210 may be operable to reduce the hardness of the contaminated fluid 201. In some embodiments, the concentration reactor 210 may include ∼100 gallons / tank and may further include a diameter of 6 feet. The concentration reactor 210 may have a retention rate of about 1 minute.

[0097] In some embodiments, the concentration reactor 210 may be in fluid communication with the filtration unit 220. A pump 216 may be provided therebetween. The pump 216 may be configured to drive and / or regulate the flow of the concentrated fluid 213 from the concentration reactor 210 to the filtration unit 220. In some embodiments, the filtration unit 220 may be provided downstream of the concentration reactor 210 and further downstream of the pump 216. The filtration unit 220 may be operable to filter contaminants from the concentrated fluid 213. In some embodiments, the filtration unit 220 may be a ceramic membrane system. A discharge flow 221 may be coupled or otherwise connected to the filtration unit 220. The discharge flow 221 may include the treated fluid 223 from the filtration unit 220.

[0098] Fluid treatment system 200, according to some embodiments, may recirculate fluid 225 from filtration unit 220 back to concentration reactor 210. The recirculation fluid 225 may be recirculated via recirculation stream 240. Recirculation stream 240 may be configured to receive the recirculation fluid 225 from filtration unit 220 and to provide the recirculation fluid 225 to concentration reactor 210. In some embodiments, a recirculation valve may be disposed on recirculation stream 240 and further configured to control the flow of the recirculation fluid 225 from the filtration unit 220 to the concentration reactor 210.

[0099] In some embodiments, the fluid treatment system 100 may include a discharge stream 231 disposed on the recirculation stream 240. The discharge stream 231 may be configured to discharge at least a portion of the recirculation fluid 225 from the recirculation stream 240. For example, the discharge stream 231 may be configured to intermittently or continuously blow down the recirculation loop to remove accumulated solids. A discharge valve 230 may be disposed on the discharge stream 231 and may be further configured to control the flow of the discharge stream 231. The recirculation fluid 241 (the recirculation fluid 225 following discharge at the valve 230) continues to the reactor 210.

[0100] The tank 210 may be oriented vertically. The inlet stream 202 may cross the walls of the tank 210, rise at least partially within the tank 210, turn through a U-turn 204, and terminate at the inlet 205. Depositing the contaminated media within the tank 210 at a relatively high position (e.g., above the midpoint of the vertically oriented tank 210) and / or away from the media outlet 214 (e.g., on the opposite side) may desirably contribute to blending and / or purification. The filtration unit 220 may be positioned as desired relative to the tank 210. For example, the filtration unit 220 may be positioned generally in the same horizontal plane as the pump 216 and / or the tank's outlet 214. The recirculation stream 240 may also desirably be poured into the tank at a relatively high position (e.g., above the midpoint of the vertically oriented tank 210) and / or away from the media outlet 214 (e.g., on the opposite side). The media outlet 214 may desirably be located relatively low within the tank 210 (eg, at the bottom, near the bottom, below the midpoint, etc.).

[0101] A particular example embodiment of a fluid treatment system is illustrated in FIG. 3. FIG. 3 illustrates a fluid treatment system 300 that may be operable to treat a contaminated fluid. System 300 includes an inlet 302, a high solids contactor 310, a pump 316, a filtration unit 320, a discharge (permeate) stream 322, and a recycle stream 340. Fluid treatment system 300 may be configured for contaminant removal. As seen in FIG. 3, fluid treatment system 300 may include a feed stream 303. Feed stream 303 may contain contaminated fluid 301 therein. System 300 may further include a skid 370 to which other components of system 300 may be secured. System 300 may further include a controller 380 and / or flow regulators, flow meters, discharge valves, flanges, and other components shown.

[0102] Sample data Table 1 illustrates sample results of fluid processing according to certain embodiments of the present disclosure. Data for five exemplary samples is shown in Table 1.

[0103] [Table 1] As will be understood by one of ordinary skill in the art having the benefit of this disclosure, other equivalent or alternative compositions, apparatus, methods and systems for fluid treatment systems may be envisioned without departing from the description contained herein. Accordingly, the modes of carrying out the disclosure shown and described are to be construed as illustrative only.

[0104] Those skilled in the art can make various changes in the shape, size, number and / or configuration of parts without departing from the scope of the present disclosure. For example, the location and number of valves or pumps can be changed. In addition, the size of the device and / or system can be scaled up (e.g., for use in a larger fluid processing system) or scaled down (e.g., for use in a miniaturized fluid processing system) to meet the needs and / or desires of the practitioner. Each disclosed method and method step can be performed concomitantly with any other disclosed method or method step and in any order according to some embodiments. Where the modal verb "may" appears, it is intended to convey an optional and / or optional condition, but its use is not intended as implying any lack of operability unless otherwise indicated. Those skilled in the art can make various modifications in the methods of preparing and using the compositions, devices and / or systems of the present disclosure.

[0105] Also, where ranges are provided, the disclosed endpoints can be treated as exact and / or approximate values ​​as desired or required by a particular embodiment. When endpoints are approximate, the degree of applicability can vary in proportion to the size of the range. For example, in the context of a range of about 5 to about 50, on the one hand, a range endpoint of about 50 can include 50.5, but not including 52.5 or 55, and in the context of a range of about 0.5 to about 50, on the other hand, a range endpoint of about 50 can include 55, but not including 60 or 75. Additionally, in some embodiments, it may be desirable to mix and match range endpoints. Also, in some embodiments, each figure disclosed (e.g., in one or more of the examples, tables, and / or figures) can form the basis and / or range endpoints of a range (e.g., the depicted value + / - about 10%, the depicted value + / - about 50%, the depicted value + / - about 100%, etc.). With respect to the former, the value of 50 depicted in the examples, tables and / or figures can form the basis of ranges, for example, from about 45 to about 55, from about 25 to about 100, and / or from about 0 to about 100.

[0106] All or part of the devices and / or systems for the fluid processing system may be constructed and arranged to be disposable, usable, replaceable and / or interchangeable. These equivalents and alternatives, together with obvious variations and modifications, are intended to be included within the scope of the present disclosure. Accordingly, the above disclosure is intended to be illustrative, but not limiting, of the scope of the present disclosure, which is illustrated by the appended claims.

[0107] The title, abstract, background, and headings are provided in compliance with regulations and / or for the convenience of the reader, and do not contain any admission as to the scope and content of the prior art, nor do they contain any limitations applicable to all disclosed embodiments. [Item 1] 1. A system for decontamination comprising: a supply stream configured to provide a contaminated fluid; a high solids catalytic reactor configured to receive the contaminated fluid from the feed stream, the high solids catalytic reactor operable to allow for formation of solids of one or more contaminants; a filtration unit configured to receive the concentrated fluid from the reactor, the filtration unit operable to filter contaminants from the concentrated fluid; a permeate operable to receive the treated fluid from the filtration unit; A system including: [Item 2] 2. The system of claim 1, wherein the filtration unit is a ceramic membrane system. [Item 3] 2. The system of claim 1, wherein the reactor is further operable to reduce the hardness of the contaminated fluid by precipitating metals from the contaminated fluid. [Item 4] 4. The system of claim 3, wherein the metals include calcium and magnesium. [Item 5] 2. The system of claim 1, further comprising an aeration unit upstream of the reactor. [Item 6] 6. The system of claim 5, wherein the aeration unit is operable to remove CO2 content from the contaminated fluid. [Item 7] 6. The system of claim 5, wherein the aeration unit includes a dissolved oxygenator, the dissolved oxygenator operable to receive compressed air from a compressed air inlet. [Item 8] 8. The system of claim 7, wherein the compressed air inlet is connected to a permeate side of the dissolved oxygenator. [Item 9] 8. The system of claim 7, wherein the dissolved oxygenator comprises a substrate having holes less than 1 micron in diameter. [Item 10] 2. The system of claim 1, further comprising a chemical inlet upstream of the reactor, the chemical inlet configured to provide at least one coagulant to the contaminated fluid, the coagulant promoting coagulation of contaminants within the contaminated fluid. [Item 11] Item 11. The system of item 10, wherein the at least one coagulant is selected from the group including alum (aluminum sulfate), ferric chloride or ferric sulfate, polyaluminum chloride (PAC) and aluminum chlorohydrate (ACH), and combinations thereof. [Item 12] 2. The system of claim 1, further comprising a chemical inlet upstream of the reactor, the chemical inlet configured to provide at least one base to the contaminated fluid in an amount sufficient to facilitate removal of metals and / or hardness from the contaminated fluid. [Item 13] Item 13. The system of item 12, wherein the at least one base is selected from the group consisting of calcium hydroxide, sodium hydroxide, potassium hydroxide, and combinations thereof. [Item 14] 13. The system of claim 12, wherein the chemical inlet upstream of the reactor is further configured to add sufficient base to raise a pH. [Item 15] 2. The system of claim 1, further comprising a pump disposed between the reactor and the filtration unit, the pump configured to regulate a flow of the concentrated fluid from the reactor to the filtration unit. [Item 16] 2. The system of claim 1, further comprising a recirculation stream configured to receive a recirculation fluid from the filtration unit and provide the recirculation fluid to the reactor. [Item 17] 20. The system of claim 16, further comprising a recirculation valve disposed on the recirculation flow, the recirculation valve configured to control a flow of the recirculation fluid from the filtration unit to the reactor. [Item 18] 17. The system of claim 16, further comprising a discharge stream disposed on the recirculation stream, the discharge stream configured to discharge at least a portion of the recirculation fluid from the recirculation stream. [Item 19] 20. The system of claim 18, further comprising a discharge valve disposed on the discharge stream, the discharge valve configured to control the flow of the discharge stream. [Item 20] 2. The system of claim 1, wherein the reactor comprises 100 gallons per tank. [Item 21] 2. The system of claim 1, wherein the reactor comprises a diameter of 6 feet. [Item 22] 2. The system of claim 1, wherein the reactor comprises a retention time of about 1 minute. [Item 23] 1. A method for decontamination comprising: receiving the contaminated fluid in a high solids catalytic reactor; reducing the hardness of the contaminated fluid in the reactor by precipitation; transferring the concentrated fluid from the reactor to a filtration unit; removing precipitate in said filtration unit; transferring the treated fluid from the filtration unit to a permeate stream; The method includes: [Item 24] 24. The method of claim 23, wherein the filtration unit is a ceramic membrane system. [Item 25] 24. The method of claim 23, wherein reducing the hardness of the contaminated fluid comprises precipitating metals from the contaminated fluid. [Item 26] 26. The method of claim 25, wherein the metals include calcium and magnesium. [Item 27] 24. The method of claim 23, further comprising removing CO2 content from the contaminated fluid using an aeration unit located upstream of the reactor. [Item 28] 28. The method of claim 27, wherein the aeration unit comprises a dissolved oxygenator. [Item 29] 28. The method of claim 27, further comprising receiving compressed air from a compressed air inlet at the aeration unit. [Item 30] 30. The method of claim 29, further comprising connecting the compressed air inlet to the permeate side of a dissolved organic compound addition device. [Item 31] 29. The method of claim 28, wherein the dissolved oxygenator comprises a substrate having holes with diameters of less than 1 micron. [Item 32] passing compressed air through the substrate; forming sub-micron sized bubbles on the wetted side of the substrate; washing the submicron sized bubbles at a flow rate of about 4 liters / minute; 32. The method of claim 31, further comprising: [Item 33] providing a chemical inlet upstream of the reactor; providing at least one coagulant to the contaminated fluid via the chemical inlet; 24. The method of claim 23, further comprising: wherein the coagulant promotes coagulation of contaminants within the contaminated fluid. [Item 34] 34. The method of claim 33, wherein the at least one coagulant is selected from the group including alum (aluminum sulfate), ferric chloride or ferric sulfate, polyaluminum chloride (PAC) and aluminum chlorohydrate (ACH), and combinations thereof. [Item 35] providing a chemical inlet upstream of the reactor; providing at least one base to the contaminated fluid via the chemical inlet; 24. The method of claim 23, further comprising: [Item 36] 36. The method of claim 35, wherein the at least one base is selected from the group consisting of calcium hydroxide, sodium hydroxide, potassium hydroxide, and combinations thereof. [Item 37] 36. The method of claim 35, wherein the step of providing at least one base further comprises adding sufficient base to raise the pH. [Item 38] providing a pump between the reactor and the filtration unit; regulating the flow of the concentrated fluid from the reactor to the filtration unit using the pump; 24. The method of claim 23, further comprising: [Item 39] providing a recirculation flow; receiving a recirculation fluid from the filtration unit in the recirculation flow; providing the recycle fluid in the recycle stream to the reactor; 24. The method of claim 23, further comprising: [Item 40] providing a recirculation valve on the recirculation flow; regulating the flow of the recirculation fluid from the filtration unit to the reactor using the recirculation valve; 40. The method of claim 39, further comprising: [Item 41] providing a discharge stream onto the recirculation stream; discharging at least a portion of the recirculation fluid from the recirculation stream via the discharge stream; 40. The method of claim 39, further comprising: [Item 42] providing a discharge valve on the discharge stream; regulating the flow of the exhaust stream using the exhaust valve; 42. The method of claim 41, further comprising:

Claims

1. 1. A system for treating a contaminated fluid to produce a treated fluid having a reduced metals content, comprising: a feed stream in fluid communication with the aeration unit and configured to provide the contaminated fluid to the aeration unit; an aeration unit having a compressed gas inlet connected to a dry side of a dissolved oxygen adder comprising a substrate having a wet side and holes having diameters less than 1 micron, the aeration unit being configured to produce an aerated fluid stream at a flow rate by discharging a gas comprising one of air and oxygen from the compressed gas inlet at a compressed gas flow rate such that the gas passes through the substrate; a chemical inlet disposed downstream of the aeration unit and configured to meter an additive into the aerated fluid stream; a high-solids contacting reactor having a reaction tank disposed downstream of the chemical inlet and configured to receive the aerated fluid stream containing the additive and retain it for a residence time to produce a concentrated stream, the high-solids contacting reactor having accumulated solids to facilitate further reaction, the high-solids contacting reactor including an inlet flow that crosses a wall of the reaction tank, rises at least partially within the reaction tank, turns through a U-turn, and terminates at an inlet such that contaminated media accumulates above a midpoint of the vertically oriented reaction tank; and an outlet located below the midpoint of the reaction tank. a filtration unit having a ceramic membrane disposed downstream of and in fluid communication with the reaction tank such that the filtration unit is configured to receive and filter the concentrate stream comprising an entire amount of the aerated fluid stream including the additive to produce a treated fluid; Equipped with the aeration unit is in fluid communication with the feed stream such that the feed stream passes through or through the aeration unit and receives at least one of micron-sized and sub-micron-sized bubbles from the aeration unit to produce an aerated feed stream; the at least one of the micron-sized bubbles and the sub-micron-sized bubbles are generated on the wetted side of the substrate; The additive comprises at least one of a coagulant and a hydroxide precipitant; system.

2. the chemical inlet is configured to provide at least one base to the contaminated fluid in an amount sufficient to facilitate removal of a plurality of metals from the contaminated fluid; The chemical inlet upstream of the reaction tank is further configured to add sufficient base to raise the pH. The system of claim 1 .

3. At least one of the hydroxide precipitants is selected from the group including calcium hydroxide, sodium hydroxide, and potassium hydroxide, and combinations thereof.

3. A system according to claim 1 or 2.

4. At least one of the coagulants is selected from the group including alum (aluminum sulfate), ferric chloride or sulfate, polyaluminum chloride (PAC) and aluminum chlorohydrate (ACH), and combinations thereof; A system according to any one of claims 1 to 3.

5. Further comprising a pump disposed between the reaction tank and the ceramic membrane filtration unit. A system according to any one of claims 1 to 4.

6. the pump is configured to regulate the flow of the concentrate stream from the reaction tank to the filtration unit. The system of claim 5.

7. a discharge stream configured to discharge at least a portion of the fluid from the filtration unit; a discharge valve disposed on the discharge flow; Further comprising: The exhaust valve is configured to control the flow of the exhaust stream. A system according to any one of claims 1 to 6.

8. The reaction tank comprises a 378.5412 liter tank. A system according to any one of claims 1 to 7.

9. The reaction tank has a diameter of 1.8288 m. A system according to any one of claims 1 to 8.

10. The residence time is 1 minute. A system according to any one of claims 1 to 9.

11. 1. A method for treating a feed stream containing a contaminated fluid to produce a treated fluid having a reduced metal content, comprising: passing or passing the feed stream through an aeration unit to produce an aerated fluid stream, the aeration unit having a dissolved oxygen adder including a substrate connected to a compressed gas inlet and having holes with diameters less than 1 micron, the aeration unit being in fluid communication with the feed stream, the feed stream receiving at least one of micron-sized and sub-micron-sized bubbles from the aeration unit, releasing a gas including one of air and oxygen from the compressed gas inlet connected to a dry side of the dissolved oxygen adder to produce the at least one of the micron-sized and sub-micron-sized bubbles on the wet side of the substrate, the plurality of bubbles being dislodged from the wet side of the substrate by the contaminated fluid flowing such that the gas passes through the substrate to produce a plurality of bubbles in the contaminated fluid; metering an additive comprising at least one of a coagulant and a hydroxide precipitant into the aerated fluid stream through a chemical inlet; receiving the aerated fluid stream containing the additive into a high solids catalytic reactor having a reaction tank; retaining the aerated fluid stream containing the additive in the reaction tank for a residence time to produce a concentrate stream; filtering the concentrate stream, which comprises the entirety of the aerated fluid stream including the additive, using a filtration unit having a ceramic membrane to produce the treated fluid; having The high-solids catalytic reactor has accumulated solids to promote further reaction, the high-solids catalytic reactor having an inlet flow that crosses the wall of the vertically oriented reactor tank, rises at least partially within the reactor tank, turns through a U-turn, and terminates at an inlet, such that contaminated media accumulates above the midpoint of the vertically oriented reactor tank, and an outlet located below the midpoint of the reactor tank; Receiving the aerated fluid stream containing the additive into the high solids catalytic reactor comprises receiving the aerated fluid stream containing the additive through the inlet stream; the concentrate stream is discharged from the reaction tank through the outlet to the filtration unit; the pressure of the gas is greater than the pressure of the contaminated fluid; method.

12. At least one of the hydroxide precipitants is selected from the group including calcium hydroxide, sodium hydroxide, and potassium hydroxide, and combinations thereof. The method of claim 11.

13. The plurality of bubbles are detached from the wetted side of the substrate by the contaminated fluid flowing at a flow rate of 4 L / min.

13. The method according to claim 11 or 12.

14. The metals include calcium and magnesium.

14. The method according to any one of claims 11 to 13.

15. The residence time is 1 minute.

15. The method according to any one of claims 11 to 14.

16. At least one of the coagulants is selected from the group including alum (aluminum sulfate), ferric chloride or sulfate, polyaluminum chloride (PAC) and aluminum chlorohydrate (ACH), and combinations thereof; 16. The method according to any one of claims 11 to 15.

17. and regulating the flow of the concentrate stream from the reaction tank to the filtration unit using a pump located between the reaction tank and the filtration unit.

17. The method according to any one of claims 11 to 16.

18. Discharging at least a portion of the fluid from the filtration unit through a discharge stream; and further comprising regulating the flow of the exhaust stream using an exhaust valve disposed along the exhaust stream.

18. The method according to any one of claims 11 to 17.

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