Treatment of iron contaminated liquids with an activated iron solids (AIS) process

Abstract

The present invention is a method and system for treating iron-contaminated water (e.g., mine drainage) using an innovative treatment approach identified herein as the Activated Iron Solids (AIS) Process. The AIS process is capable of oxidizing and removing iron as iron oxides from iron-contaminated waters (such as, mining-related discharge, groundwater, surface water and industrial waste streams) producing a clean effluent. The AIS process is performed in a single or multiple tank system in which a catalytic surface chemistry process increases the iron removal 1000s times faster than would naturally occur and 100s of times faster than existing arts (e.g., aerobic pond passive treatment). In addition, the AIS process can utilize inexpensive alkaline material (such as, pulverized limestone) where initial mine drainage alkalinity (mg/L as CaCO3) to ferrous iron (mg/L) ratio is less than approximately 1.7. Excess accumulated iron oxides are periodically removed from the systems using a waste activated iron solids (WAIS) system and is directed to an Iron Oxide Thickener where the iron oxides are further concentrated.

Description

RELATED APPLICATION

This patent application is a continuation in part to a pending patent application, entitled, “A process and System for Treating Iron Contaminated Liquids” filed Jun. 3, 2003, Ser. No. 10/453,127, which claims priority from a provisional patent application entitled, “A Process and Device for Treating Iron Contaminated Liquids” filed Jun. 3, 2002, Ser. No. 60/384,680.

BACKGROUND OF THE INVENTION

1. Field of the Invention

This invention relates generally to a device and method for and the treatment of iron-contaminated fluid (e.g., mining-related discharge, groundwater, surface water and industrial waste streams) and, more particularly, to an apparatus and method for oxidizing and removing ferrous iron from iron-contaminated fluid, including mine drainage, and producing an effluent substantially free of iron.

2. Description of the Prior Art

Iron-contaminated water result from a variety of natural and anthropogenic processes with the later typically involving mining and industrial processing. Ferrous iron is released from minerals (e.g., pyrite, siderite, and hematite) through dissolution and redox processes. Industrial processing typically involves formation of reduced iron (Fe⁰) into various metallic compounds, with waste streams or subsequent oxidation causing elevated ferrous iron levels.

The most common source of iron-contaminated water results from mineral extraction and can be produced from either surface or deep mining practices where iron sulfide minerals contained in the minerals and surrounding formations are oxidized. The chemistry of mine drainage will vary depending on overburden characteristics and mining and reclamation techniques. In the United States millions of gallons of mine drainage is produced daily from both active and abandoned mine sites. Treating mine drainage is an expensive endeavor involving land, construction, materials, operation, maintenance and chemical costs. Left untreated, mine drainage contaminants surface and groundwater causing impacts to their social, recreational and commercial uses.

Iron is removed from iron-contaminated waters employing chemical and passive treatment technologies. Current chemical treatment, more commonly used for industrial sources and active mines, requires continuous metering of caustic chemicals (e.g., lime, hydrated or soda ash) to raise the pH above 8 thereby increasing the rate of iron oxidation and precipitation as oxides (USEPA 1981). In addition to chemical additives, active treatment requires an assorted array of pumps, aeration equipment and multiple oxidation and settling basins. Iron oxide solids produced in chemical treatment are low density (1 to 4% solids) and highly contaminated with calcium, aluminum, manganese, and sodium deposits (Dempsey & Jeon 2001). The low-density solids slowly settle in large open water basins, which require frequent and costly maintenance to remove and dispose the accumulated solids.

Passive treatment systems rely on natural amelioration processes that do not require pumps or metered chemical additions. In general, mine drainage passes through open water ponds and/or aerobic wetlands where abiotic and biotic processes contribute to the oxidation and precipitation of iron (Hedin & Nairn 1993). Iron removal in passive treatment systems require much larger land areas (10 to 20 times greater) than chemical treatment, which can become excessive for high flow and/or high iron concentration mine drainage discharges. In addition, iron removal in passive systems can be problematic with performance varying with season, influent flow and concentration. Iron oxide solids produced by passive treatment systems have much higher sludge density (15-30%) than chemical treatment and are frequently less contaminated (Dempsey & Jeon, 2001). Reported iron oxide content in passive treatment solids varies from 50 to 90%.

AIS-treated waters produce a unique iron oxide sludge that (1) settles at a rate faster than either chemically or passively produced solids; (2) is a high-density sludge with solids of approximately 30%; and (3) is a high-purity sludge with iron oxide content exceeding 95%. The prior art does not address the unique solids content of AIS-treated fluids.

Ferrous iron oxidation is usually the limiting step in the iron removal from iron-contaminated mine drainage. Iron oxidation has been described to occur by two separate processes known as homogeneous oxidation, a solution oxidation process, and heterogeneous oxidation, a solid/solution interface oxidation process. Homogeneous oxidation involves soluble Fe²⁺, FeOH⁺, or Fe(OH)₂^o species in the presence of dissolved oxygen (Stumm & Morgan 1996). This oxidation is strongly dependent on pH with slow oxidation occurring at pH 6 and rapid oxidation occurring above pH 8. Heterogeneous oxidation involves sorbed ferrous iron on the surface of iron oxides in which the iron oxide acts as a catalyst (Dietz 2003 and Tamura & Nagayama 1976). At high iron oxide concentrations, heterogeneous oxidation has been found to produce oxidation rates greater than 100 times the rates observed in passive treatment and comparable rates to chemical treatment (Dietz 2003, and Dietz & Dempsey 2001). ). Heterogeneous ferrous iron oxidation (HeFIO) is described by the following model:

$\frac{\partial \left[\mathrm{Fe}\left(\mathrm{II}\right)\right]}{\partial t}=-\left(k_{\mathrm{He}1}\times \left[\mathrm{DO}\right]\times \frac{1+\left(\left[{\mathrm{Fe}\left(\mathrm{II}\right)}_{\mathrm{diss}}\right]\times K_1^{\mathrm{app}}\right)}{\left[\equiv \mathrm{Fe}\left(\mathrm{III}\right)\right]\times {\Gamma }_1\times {\left\{H^{+}\right\}}^1}\right)-$
$\left(k_{\mathrm{He}2}\times \left[\mathrm{DO}\right]\times \frac{1+\left(\left[{\mathrm{Fe}\left(\mathrm{II}\right)}_{\mathrm{diss}}\right]\times K_2^{\mathrm{app}}\right)}{\left[\equiv \mathrm{Fe}\left(\mathrm{III}\right)\right]\times {\Gamma }_2\times {\left\{H^{+}\right\}}^2}\right)$
${\mathrm{pK}}_{x,T2}^{\mathrm{app}}={\mathrm{pK}}_{x,T1}^{\mathrm{app}}-\left(\frac{{\mathrm{\Delta H}}_{\mathrm{rxn},x}^0}{2.303\times R}\times \frac{T_2-T_1}{T_2\times T_1}\right)$
${\mathrm{pk}}_{\mathrm{Hex},T2}={\mathrm{pk}}_{\mathrm{Hex},T1}-\left(\frac{E_{a,x}}{2.303\times R}\times \frac{T_2-T_1}{T_2\times T_1}\right)$
Summary of parameters and constants in the ferrous iron sorption
heterogeneous ferrous iron oxidation (HetOX) models.
		Sub-	Sub-
		Model	Model
Model Parameter	Description	(x = 1)	(x = 2)
[Fe(II)]	Ferrous Iron Concentration, molar	varies	Varies
∂[Fe(II)]/∂t	Ferrous Iron Oxidation Rate	varies	varies
[DO]	Dissolved Oxygen Concentration,	varies	varies
	molar
[Fe(II)]diss	Dissolved Fraction of Ferrous Iron,	varies	varies
	molar
[≡Fe(III)]	Suspended AIS as Ferric Iron	varies	varies
	Concentration, g/L
{H+}	Hydrogen Ion Activity, molar	varies	varies
	{H+} = 10−pH
kHex (M−1s−1)	Oxidation Rate Constant	0.105	38.0
Ea,x (kJ/mol)	Activation Energy of Oxidation	60.7	60.7
	Reaction
Kxapp (Mx−1)	Surface Complexation Constant	10−1.265	10−10.78
Γx (mol/mol)	Sorption Site Density	0.0045	0.212
ΔH0rxn,x (kJ/mol)	Enthalpy of Sorption Reaction	69.0	96.2
{H+}	Hydrogen Ion Coefficient	1	2
Coefficient (x)

Homogeneous oxidation is by far the dominant process in both chemical and passive treatment, typically accounting for greater than 95% of the oxidation. This occurs because (1) chemical treatment occurs at high pH were homogeneous oxidation is by far the fastest oxidation either with or without suspended iron oxide solids; and (2) passive treatment is a non-mechanical approach that does not allow for the suspension of high concentrations of iron oxide (>200 mg/L) that would be needed to have heterogeneous dominated ferrous iron oxidation.

Alkalinity may need to be generated to complete the precipitation of oxidized ferrous iron where the source water alkalinity (mg/L as CaCO₃) to iron (mg/L as Fe) ratio is less 1.7. The low pH (approximately 5 to 6) and/or high carbonic acid concentrations (P_CO2 approximately 0.1 to 0.5) found in many iron-contaminated waters (i.e., mine drainage) results in the rapid dissolution of carbonate minerals (such as calcite), thereby producing alkalinity at concentrations higher than will typically occur in natural systems. A type of passive treatment, known as Anoxic Limestone Drains (ALD), has been found to produce alkalinity greater than 300 mg/L (Hedin et al 1994). Other research has found carbonate dissolution occurs rapidly until pH greater than 6 is achieved and the rate of dissolution is directly proportional to the surface area of the carbonate mineral present (Amrhein et al 1985; Pearson & McDonnell 1974). Testing done with a relatively unused material, pulverized limestone, in AIS treatment has been shown to adequately address the alkalinity issue due to rapid dissolution of the carbonate in the high ferrous oxidation reaction rate environment of AIS in combination with the complete mixing in the AIS reactor.

Therefore, it is the object of this invention to provide a treatment processes and apparatus to oxidize and remove ferrous iron from iron-contaminated mine waters at pH (less than 7) typically found in iron-contaminated waters.

Another object of this invention is to oxidize and remove ferrous iron from iron-contaminated waters by using the higher oxidation rates supported by heterogeneous oxidation and providing a source of alkalinity where inadequate alkalinity is present to complete the oxidation and precipitation of iron.

It is also an object of this invention to develop a simple means of collecting and concentrating the iron oxides produced by the iron-contaminated liquid treatment processes and apparatuses.

Other objects will be readily apparent after reading the description and reviewing the figures described below.

SUMMARY OF INVENTION

The invention involves an apparatus consisting of a single tank or multiple tank assembly (in series or parallel) containing aeration and/or mixing apparatus, storage capacity for activated iron solids (AIS), a method of concentrating iron oxides in the reactor, time and/or flow-based process controls, and a waste activated iron solids (WAIS) apparatus. The invention also includes apparatus to add alkaline material (such as, pulverized calcite limestone) directly to the container assembly where additional alkalinity is needed to complete the ferrous iron oxidation and precipitation reactions and a separate container assembly to thicken iron oxides produced by the treatment process. The invention has the capacity to discharge substantially iron free water with circumneutral pH.

The following description will provide a complete understanding of the invention when reviewed in connection with the accompanying drawing figures.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a schematic plan view of a preferred treatment system for oxidizing and removing ferrous iron from a flow of iron-contaminated mine water.

FIG. 2 is a schematic cross-sectional view of a preferred embodiment of the AIS container assembly.

DESCRIPTION OF PREFERRED EMBODIMENTS

FIG. 1 is a plan view of the treatment system. An iron-contaminated water source (1) is directed into a least one AIS container assembly (4) or more preferably a plurality of AIS container assemblies. The means of directing the iron-contaminated water into at least one AIS container assembly may be by gravitational force or by pumping the iron-contaminated liquid into the AIS container assembly. When a plurality of AIS container assemblies are used in the treatment of iron-contaminated water, a means for collecting and distributing the iron-contaminated water, such as a header system or distribution tank assembly, precedes the AIS/container assembly (3).

The source of iron-contaminated fluid is directed through a first conduit (2) that is engaged with the inlet of the AIS container assembly (4) or a plurality of AIS container assemblies. Each AIS container assembly in a plurality of AIS container assemblies is identical as shown in FIGS. 2a and 2b, a cross-section view of the AIS container assembly. FIG. 2a is a sequencing batch reactor (SBR) container assembly where all processes (fill, react, flocculation, settling, AIS retention, decant, and AIS wasting) occur sequentially within one (1) container assembly. FIG. 2b is a flow-through container assembly having (1) at least two completely stirred reactors (CSTR) in series; (2) an upflow reactive bed clarifier following the CSTR; and (3) a system in the upflow reactive bed clarifier to re-circulate and waste AIS. The container assembly method includes:

A system of the present invention has the following features:

• • 1) A means for directing the fluid to be treated into a container assembly having the features described herein;
  • 2) A means of aeration and mixing within the container assembly to provide sufficient oxygen for ferrous iron oxidation, carbon dioxide removal for optimal pH operation, and suspension of the activated iron solids (AIS) in solution;
  • 3) A means of storing or re-circulating AIS within the container assembly to maintain sufficiently high reactor iron oxide concentrations to catalyze ferrous iron oxidation;
  • 4) A means of decanting or overflow from the container assembly to remove treated iron-contaminated fluid;
  • 5) A means to remove excess iron oxides from the container assembly; and
  • 6) A means of controlling the duration of the various container assembly processes such as fill, reaction, flocculation, settling and decant. Such means include may include any of the commercially available means (e.g., the Tork adjustable cycle timer, the Tyco Time Delay Relays, the Ametek National Controls Corporation Multi-range Delay on Break or the Grasslin Timemaster GMX Series 24 hr 7 day cycle timer).

The method of the present invention includes the following steps:

• • 1) Directing a fluid to be treated into a container assembly having the features described herein;
  • 2) Aerating and mixing iron-contaminated fluid within a container assembly to provide sufficient oxygen for ferrous iron oxidation, carbon dioxide removal, and suspension of the activated iron solids (AIS) in solution;
  • 3) Storing or re-circulating AIS within the container assembly to maintain sufficiently high reactor iron oxide concentrations to catalyze ferrous iron oxidation;
  • 4) Decanting the container assembly to remove treated iron-contaminated fluid;
  • 5) Removing excess iron oxides from the container assembly; and
  • 6) Controlling the duration of the various container assembly processes such as fill, reaction, flocculation, settling and decant to optimize the process and desired output characteristics. Commercially available timers and controls are described above.

The method may also include a plurality of container assemblies operated with an inlet header and a means for selectively isolating the flow to selected container assemblies. Processing steps in the AIS/SBR Container assembly are described below:

Fill Step. Iron-contaminated fluid enters at least one AIS/SBR tank assembly. Preferably, for an efficient process, the tank is filled to capacity with such iron-contaminated fluid. In some preferred embodiments the iron-contaminated fluid is mixed, aerated or both during the fill step. The temporal duration of the fill step may vary depending on fluid flow rate and characteristics, tank volume and the chemistry of the iron-contaminated fluid. Commercially available floats and relay switches may be used in this step.

Alkaline Addition Optional Step. Alkaline material optionally may be added to an AIS/SBR tank assembly after or during the fill step preferably using a doser assembly (5 on FIG. 1). The amount of alkaline material added to the iron-contaminated fluid in the AIS/SBR tank assembly may vary depending on the chemistry of the iron-contaminated fluid and the amount of alkalinity needed to complete iron precipitation. A commercially available timer and control may be used in this step.

React Step. Oxidation and precipitation occurs in an AIS/SBR tank assembly during the react step. In addition, in cases in which alkaline material is added, the dissolution of the material and the generation of alkalinity occur in conjunction with the oxidation and precipitation of iron. Iron oxides retained in the AIS/SBR Tank Assembly are suspended in fluid providing a surface for heterogeneous ferrous iron oxidation. Iron oxides in suspension during the react step for mine drainage typically range from approximately 500 up to 5,000 mg/L as iron and depend on the chemistry of the iron-contaminated fluid and the mixed fluid in the AIS/SBR tank assembly during the react step. Precipitation of ferric iron produced from the oxidation of ferrous iron is rapid and requires much less time than the ferrous iron oxidation. React durations will vary depending on iron-contaminated fluid ferrous iron concentration, the volume of iron-contaminated fluid to be treated, pH, dissolved oxygen and alkalinity. When the iron-contaminated fluid is mine drainage and standard AIS/SBR tank assemblies are used, the duration of the react period is generally less than two hours.

Flocculation Optional Step. AIS and new iron oxides formed during the react step may benefit from an optional flocculation step to create larger iron oxide particles that settle more readily and easily. The optional flocculation step involves slow mixing to provide a fluid velocity in the reactor equal to or less than 0.001 ft/sec in an AIS/SBR tank assembly to enable iron oxide particle interaction and agglomeration. Flocculation durations vary depending on the desired output and characteristics of the fluid and particles after the react step. When treating iron-contaminated mine drainage in standard AIS/SBR tank assemblies, this step may last as long as one-half hour in duration. A commercially available timer and control may be used in this step.

Settle Step. Iron oxides are removed from suspension in the AIS/SBR tank assembly by substantially ceasing and mixing or aeration treatment of the iron-contaminated fluid. The substantially quiescent conditions in the AIS/SBR Tank Assembly permit AIS and newly formed iron oxides to settle and accumulate in the bottom of an AIS/SBR tank assembly. Settle step durations vary depending on the AIS concentration in the AIS/SBR tank assembly and desired purity of the resulting fluid. When treating iron-contaminated mine drainage in standard AIS/SBR assemblies, this step generally is less than two hours in duration. A commercially available timer and control may be used in this step.

Decant Step. Subsequent to the settle step, treated fluid in an AIS/SBR tank assembly is removed from the tank assembly during the decant step. The decant step involves the removal, preferably rapid removal, of substantially clarified supernatant fluid that overlies fluid containing settled AIS. Typically, less than 75% of the fluid in the tank is decanted although both the volume and time of the decant step will vary depending on the desired characteristics of the decanted fluid, the volume of the tank and the rapidity and thoroughness of the settling step. In a preferred embodiment for treating iron-contaminated water, the decant period to remove 75% of the volume of the fluid in the tank wherein the tank is a standard volume, the mine drainage has standard characteristics, the time for the decant step generally is less than one-half hour and is determined based on a per cent of tank drawdown. Commercially available floats and relay switches may be used in this step.

AIS Wasting Step. Excess AIS that results from newly formed iron oxides, periodically are removed from the AIS/SBR tank assembly in a step known as AIS wasting. AIS wasting may occur during any of the above steps and optionally can be conducted during a plurality of steps. The duration, volume of AIS removed, purity of AIS removed and frequency of this step will vary depending on the characteristics of the iron contaminated fluid to be treated, the application and duration of the other steps, the use of optional steps, and the desired characteristics of effluent. A commercially available timer and control may be used in this step.

Steps in the process using two-stage flow-through AIS container assembly comprise:

• • 1) Inflow step. Iron-contaminated fluidenters the AIS container assembly, preferably on a continuous basis.
  • 2) Alkaline addition optional step. Alkaline material optionally is added to the first reactor in the two-stage flow-through AIS container assembly, preferably on a continuous basis (5 on FIG. 1). The amount of alkaline material applied varies depending on the characteristics of the chemistry of the iron-contaminated fluid and the amount of alkalinity needed to complete the iron precipitation.
  • 3) Oxidation and precipitation Step. Oxidation and precipitation occurs in the first and second reactors (Stage 1 and Stage 2). Iron oxides re-circulated to the first reactor are suspended through aeration and mixing to provide a surface for the heterogeneous ferrous iron oxidation. This high iron oxide concentration preferably is maintained by flow-through in the second reactor. Iron oxides in suspension in the first and second reactors may be in the range from approximately 500 up to 3,000 mg/L as iron depending on the chemistry of the iron-contaminated fluid and the mixed fluid in the first and second reactors. Precipitation of ferric iron produced from the oxidation of ferrous iron is rapid and requires much less time than the ferrous iron oxidation. First reactor and second reactor volumes and detention times vary depending on iron-contaminated fluid flow, ferrous iron concentration, pH, dissolved oxygen and alkalinity, but usually comprises less than two hours of detention time.
  • 4) Solids removal Step. AIS and new iron oxides formed in the first and second reactors are removed and collected in the upflow reactive bed clarifier. The hydraulic design of the system allows for a suspended layer of highly concentrated iron oxides, ranging from 10,000 to 60,000 mg/L and functions as a filter separating particulate iron oxides from the flow from the second reactor. The highly concentrated layer of iron oxide continues the oxidation and precipitation of iron and can be employed as a stand-alone unit. The size of the upflow reactive bed clarifier depends on the flow and chemical characteristics of the water being treated, but is approximately in the range of 1,500 to 4,000 gallons per day for every square foot of upflow reactive bed clarifier surface area.
  • 5) AIS recirculation and wasting Step. AIS collected in the upflow reactive bed clarifier is continuously removed and re-circulated to the first reactor using a solids or air lift pump system, or a combination thereof Excess AIS, a result of newly formed iron oxides, are periodically or continuously removed from the container assembly using this recirculation system, but diverting the AIS to a holding tank or thickener.

In an embodiment of the present invention that employs this method and system, the AIS container assembly or plurality of AIS Container assemblies is connected to an outlet conduit (6 on FIG. 1) into which treated fluid is discharged from the AIS container assembly. The outlet discharges optionally into a receiving waterbody or an additional treatment system. Decant fluid or effluent from the AIS Container assembly will have pH greater than 6 and iron concentrations of 5 mg/L or less depending on the effluent criteria or treatment goals.

The method and system according to the present invention optionally includes an additional method of and system for thickening iron oxides produced by the foregoing method and system. An iron oxide thickening system comprises:

• • 1) A means of conveying fluids containing iron oxides to a container;
  • 2) A container in which fluids containing iron oxides are retained to provide additional settling time, slow mixing of the fluid to increase solids, or both;
  • 3) A means of removing concentrated iron oxide solids from the container; and
  • 4) A means of decanting supernatant substantially free of iron solids from the container.

Iron oxide thickening steps of the method of the present invention include:

• • 1) Conveying fluids containing iron oxides to a container;
  • 2) Retaining a fluid containing iron oxides in a container for sufficient time for iron oxides to concentrate in the fluid by removal of water accomplished by providing additional settling time, slow mixing of the fluid containing iron oxide to increase the removal of water, or to both settle and mix such fluids;
  • 3) Removing concentrated iron oxide solids from the container; and
  • 4) Decanting a supernatant substantially free of iron solids from the container.

In an embodiment of the present invention that employs this method and system, waste activated iron solids (WAIS), the excess AIS produced by an iron oxidation treatment method or system according to the present invention, is directed into a container. Such fluid can be directed into the container by using a variety of means including pumps, gravitational force, a combination of both, or other means. See step 7 on FIG. 1. The container and thickening step decreases the fluid content of the iron oxide solids and thereby increases the solid content of the iron oxide solids. The iron oxide thickener container system consists of a container assembly containing a supernatant decant pump and a solid recovery pump. The container assembly may also provide a means for mixing the fluid to aid in removing excess water from the iron oxide solids. Iron oxides resulting from such a step and system typically have a solid content up to 40%. Solids recovered from such processes and systems have commercial reuse potential.

It will be understood from the above description that the present invention is related to a new device and treatment process for iron-contaminated water, such as mine drainage. This process and device may decrease the treatment area or volume or construction costs compared to passive treatment approaches; and decrease treatment costs compared to conventional chemical treatment through the elimination of the use of costly chemicals (e.g., lime and polymers) or their replacement with lower cost chemicals (e.g. pulverized limestone). The process may prove to be an economical alternative to both current passive treatment and chemical treatment approaches. The process has the added benefit of producing a relatively pure and easier to recover iron oxide solid that may have commercial value.

Although preferred embodiments of the invention have been described in detail herein, it will be appreciated by those skilled in the art that various modifications and alternatives to the preferred embodiments may be developed in light of the overall teaching of the disclosure. Accordingly, the particular arrangements are illustrative only and are not limiting as to the scope of the invention, which is to be given full breadth of the amended claims and any and all equivalents thereof

Claims

1. A system for removing ferrous iron from a fluid comprising:

a. At least one first container for receiving iron-contaminated fluid wherein said first container has at least one means of ingress and egress of fluid;

b. A means of transporting iron-contaminated fluid into said first container;

c. A means of aerating and mixing iron-contaminated fluid within said first container;

d. A means of decanting substantially iron-free supernatant fluid from said first container without disturbing settled iron oxides; and

e. A means of controlling the volume and temporal duration of transporting fluids in and out of said first container, aerating and mixing a fluid within said first container, and maintaining a fluid in a quiescent state in said first container.

2. A system according to claim 1 having a plurality of first containers.

3. A system according to claim 2 further comprising a means for selectively directing the flow of a fluid to at least one of said first containers.

4. A system of claim 1, 2 or 3 further comprising a means for delivering alkaline-bearing material into said first container.

5. A system of claim 1, 2, or 3 further comprising:

a. A means for conveying fluid from a first container into a second container;

b. A means of mixing fluids in said second container;

c. A means of removing iron oxides from said second container; and

d. A means of decanting a substantially iron-free supernatant fluid from said second container.

6. A system of claim 4 further comprising:

a. A means for conveying fluid from a first container into a second container;

b. A means of mixing fluids in said second container;

c. A means of removing iron oxides from said second container; and

d. A means of decanting a substantially iron-free supernatant fluid from said second container.

7. A method of removing ferrous iron from a fluid comprising:

a. Filling at least one first container with an iron-containing fluid;

b. Aerating the fluid within a first container sufficiently to ensure ferrous iron oxidation;

c. Mixing fluid within the first container sufficiently to maintain a suspension of iron oxide solids necessary to catalyze ferrous iron oxidation;

d. Storing activated iron solids within a first container sufficiently to maintain high reactor iron oxide concentrations necessary to catalyze ferrous iron oxidation;

e. Decanting a substantially iron-free supernatant fluid from a first container; and

f. Removing excess iron oxides from a first container.

8. A method according to claim 7 wherein a plurality of first containers are filled with a fluid to be treated.

9. A method according to claim 8 further wherein fluid is selectively directed either simultaneously or sequentially into first containers for treatment.

10. A method of claim 7, 8 or 9 further comprising adding alkaline-bearing material into a first container in sufficient quantity to provide sufficient alkalinity to precipitate iron oxides in a fluid to be treated.

11. A method of claims 7, 8, or 9 further comprising:

a. Conveying fluid from a first container into a second container;

b. Mixing fluids in a second container;

c. Removing iron oxides from a second container; and

d. Decanting a substantially iron-free supernatant fluid from a second container.

12. A method of claim 10 further comprising:

a. Conveying fluid from a first container into a second container;

b. Mixing fluids in a second container;

c. Removing iron oxides from a second container

d. Decanting a substantially iron-free supernatant fluid from a second container.

13. A method of claim 7, 8 or 9 further comprising mixing fluids sufficiently to promote flocculation after said storing of activated iron solids within a first container sufficiently to maintain high reactor iron oxide concentrations necessary to catalyze ferrous iron oxidation.