Patent Description:
Generally, the application is directed towards different configurations and processes of utilizing electrolysis cells in order to provide a purified aluminum product from a feedstock containing aluminum metal. More specifically, the application is directed towards utilizing vertically oriented, interspaced anode and cathode configuration, where the anodes and cathodes are configured from aluminum-wettable material, in order to reduce inter-polar distance, and increase the electrode surface area (e.g. purification zone) of an electrolysis cell operating to produce purified aluminum metal product from an aluminum feedstock with much lower energy consumption and higher productivity (c. feedstock including an aluminum metal and/or alloys thereof). In accordance with the present invention there is provided a method for purifying an aluminum feedstock comprising:.

Preferably, prior to the feeding step, melting the feedstock material, and/or removing at least one of: sludge and raffinate from the molten metal pad zone via the cell access channel. Advantageously, the method further comprises removing the purified aluminum product from the aluminum electrolysis cell, and preferably wherein the removing step comprises tapping the aluminum electrolysis cell. Preferably, the removing step comprises casting the purified aluminum product into an ingot, wherein the ingot comprises an aluminum product having an aluminum purity of at least <NUM> wt. Conveniently, both the anode and cathode comprise an aluminum-wettable material, and/or wherein both the anode and cathode are submerged in the electrolyte. Preferably, the directing step comprises supplying the electric current to the elongate vertical anode. Advantageously, the purified aluminum product comprises an aluminum purity of from <NUM> wt. % to <NUM> wt. % Al, or wherein the purified aluminum product comprises an aluminum purity from <NUM> wt. % to <NUM> wt. % Al, or wherein the purified aluminum product comprises an aluminum purity of from <NUM> wt. % to <NUM> wt. % Al, or wherein the purified aluminum product comprises an aluminum purity of from <NUM> wt. % up <NUM> wt. Preferably, the method comprises forming a third zone wherein the third zone comprises a purified aluminum product, wherein the third zone is a top layer above the electrolyte. Advantageously, the purified aluminum product is produced via the aluminum electrolysis cell at an energy efficiency of from <NUM> to <NUM> kWh/kg of purified aluminum product, or wherein the purified aluminum product is produced via the aluminum electrolysis cell at an energy efficiency of from <NUM> to <NUM> kWh/kg of purified aluminum product, or wherein the purified aluminum product is produced via the aluminum electrolysis cell at an energy efficiency of from <NUM> to <NUM> kWh/kg of purified aluminum. Conveniently, the aluminum electrolysis cell comprises a cell chamber, the method comprising: purging the cell chamber with an inert gas. Preferably, the method comprises producing an inert headspace within the aluminum electrolysis cell, wherein the producing comprises flowing an inert gas into the aluminum electrolysis cell via an inert gas inlet, wherein the inert gas inlet is located in a refractory top cover of the aluminum electrolysis cell. Advantageously, the method comprises densifying the molten metal pad zone, wherein the densifying comprises adding densifying aids into the aluminum feedstock in order to configure the density of the aluminum feedstock for retention in the molten metal pad zone prior to the wetting step. Preferably, the method comprises adding bath components to the aluminum electrolysis cell via the cell access channel, preferably wherein the bath components supplement the electrolyte and promote the producing and reducing steps. Conveniently, the elongate vertical anode comprises at least one of TiB<NUM>, ZrB<NUM>, HfB<NUM>, SrB<NUM>, carbonaceous material, W, Mo, steel and combinations thereof and the elongate vertical cathode comprises at least one of TiB<NUM>, ZrB<NUM>, HfB<NUM>, SrB<NUM>, carbonaceous material, and combinations thereof. Preferably, due to the wetting step, the aluminum metal covers surfaces of the elongate vertical anode.

The present invention will be further explained with reference to the attached drawings, wherein like structures are referred to by like numerals throughout the several views. The drawings shown are not necessarily to scale, with emphasis instead generally being placed upon illustrating the principles of the present invention. Further, some features may be exaggerated to show details of particular components.

The figures constitute a part of this specification and include illustrative embodiments of the present invention and illustrate various objects and features thereof. Further, the figures are not necessarily to scale, some features may be exaggerated to show details of particular components. In addition, any measurements, specifications and the like shown in the figures are intended to be illustrative, and not restrictive.

Among those benefits and improvements that have been disclosed, other objects and advantages of this invention will become apparent from the following description taken in conjunction with the accompanying figures. Detailed embodiments of the present invention are disclosed herein; however, it is to be understood that the disclosed embodiments are merely illustrative of the invention that may be embodied in various forms. In addition, each of the examples given in connection with the various embodiments of the invention which are intended to be illustrative, and not restrictive.

Throughout the specification and claims, the following terms take the meanings explicitly associated herein, unless the context clearly dictates otherwise. The phrases "in one embodiment" and "in some embodiments" as used herein do not necessarily refer to the same embodiment(s), though it may. Furthermore, the phrases "in another embodiment" and "in some other embodiments" as used herein do not necessarily refer to a different embodiment, although it may. Thus, as described below, various embodiments of the invention may be readily combined, without departing from the scope or spirit of the invention.

In addition, as used herein, the term "or" is an inclusive "or" operator, and is equivalent to the term "and/or," unless the context clearly dictates otherwise. The term "based on" is not exclusive and allows for being based on additional factors not described, unless the context clearly dictates otherwise. In addition, throughout the specification, the meaning of "a," "an," and "the" include plural references. The meaning of "in" includes "in" and "on.

As used herein, "aluminum feedstock" means material having at least <NUM> wt. % aluminum.

As used herein, "purified molten aluminum" means molten material having at least <NUM> wt. % aluminum.

As used herein, "molten metal pad" means a reservoir of molten material located below an electrolyte, wherein the molten material comprises aluminum.

As used herein, "sludge" means waste material precipitated during aluminum purification. In some embodiments, sludge comprises solid material.

As used herein, "raffinate" means aluminum containing a very high impurity content.

As used herein, "aluminum-wettable" means having a contact angle with molten aluminum of not greater than <NUM> degrees.

As used herein, "electrolyte" means a medium in which the flow of electrical current is carried out by the movement of ions/ionic species. In one embodiment, an electrolyte may comprise molten salt.

As used herein, "energy efficiency" means the amount of energy (in kilowatt hours) consumed by an aluminum electrolysis cell per kilogram of purified aluminum produced by the aluminum electrolysis cell. Thus, energy efficiency may be expressed in kilowatt hours/kilogram of aluminum produced (kWh/kg).

As used herein, "anode-cathode overlap" (ACO) means the vertical distance from the distal end of an elongate vertical anode to the distal end of a respective elongate vertical cathode.

As used herein, "anode to cathode distance" (ACD) means the horizontal distance separating an elongate vertical anode from a respective elongate vertical cathode.

The present disclosure describes an aluminum electrolysis cell. The cell may include a base, refractory sidewalls, and a refractory top cover. The cell may include a bottom located proximal the base, wherein the bottom has an upper surface. The cell may include an anode connector in electrical communication with the bottom, the anode connector having an outer end configured to connect to an external power source. The cell may include an elongate vertical anode extending upward from the upper surface of the bottom. The elongate vertical anode may have a proximal end connected to the upper surface of the bottom, a distal free end extending upward toward the refractory top cover, and a middle portion. The cell may include a cathode connector proximal the refractory top cover. The cathode connector may have an upper connection rod configured to connect to the external power source, and a lower surface. The cell may have an elongate vertical cathode extending downward from the lower surface of the cathode connector. The elongate vertical cathode may have a proximal end connected to the upper surface of the cathode connector, a distal free end extending downward toward the base, and a middle portion. In one embodiment, the elongate vertical cathode overlaps the elongate vertical anode such that the distal end of the elongate vertical cathode is proximal the middle portion of the elongate vertical anode, and the distal end of the elongate vertical anode is proximal the middle portion of the elongate vertical cathode.

The aluminum electrolysis cell includes a cell chamber defined by the refractory sidewalls, the refractory top cover, and the bottom. The cell may include an access channel penetrating a lower portion of a refractory sidewall, thereby providing access to a lower portion of the cell chamber. The cell access channel may have an access port.

The aluminum electrolysis cell includes an aluminum extraction port penetrating an upper portion of a refractory sidewall, thereby providing access to an upper portion of the cell chamber. In one embodiment, the aluminum electrolysis cell includes an inert gas inlet formed in the refractory top cover configured to provide an inert atmosphere to the cell chamber.

The aluminum electrolysis cell includes an outer shell, wherein the outer shell comprises: a shell floor located beneath the base; and shell sidewalls spaced apart from and surrounding the refractory sidewalls. The aluminum electrolysis cell may include thermal insulation, wherein the thermal insulation is located between the shell floor and the base, and between the shell sidewalls and the refractory sidewalls.

The elongate vertical anode is aluminum-wettable. In this regard, the elongate vertical anode may include at least one of TiB2, ZrB2, HfB2, SrB2, carbonaceous material, W, Mo, steel and combinations thereof.

The elongate vertical cathode is aluminum-wettable. In this regard, the elongate vertical cathode may include at least one of TiB2, ZrB2, HfB2, SrB2, carbonaceous material, and combinations thereof.

Without being bound by any particular mechanism or theory, it is believed that the anode is configured to undergo an electrochemical reaction, such that the aluminum metal with impurities is anodized to aluminum ions Al<NUM>+ (transported to the electrolyte) such that impurities are left behind on the anode. Then, the ions are reduced onto the cathode surface and form aluminum metal, where the metal is in purified form, since the impurities remained on the anode surface and/or were collected in the metal pad (e.g. given density of the impurities vs. the electrolyte/bath components).

<FIG> and <FIG> are schematics of an electrolysis cell for purifying aluminum. In the illustrated example , the electrolysis cell (<NUM>) comprises a base (<NUM>), refractory sidewalls (<NUM>), and a refractory top cover (<NUM>). The aluminum electrolysis cell (<NUM>) includes a bottom (<NUM>) located proximal the base (<NUM>). The bottom (<NUM>) has an upper surface (<NUM>) and a lower surface (<NUM>). In some embodiments, the upper surface (<NUM>) of the bottom (<NUM>) is sloped. In some embodiments, the slope comprises an angle of less than <NUM> degrees. In some embodiments, the slope comprises an angle of about <NUM> to <NUM> degrees. The aluminum electrolysis cell (<NUM>) includes an anode connector (<NUM>). The anode connector (<NUM>) is in electrical communication with the lower surface (<NUM>) of the bottom (<NUM>). In some aspects , the bottom includes at least one slot configured to receive the anode connector. The anode connector (<NUM>) has an outer end (<NUM>) configured to connect to an external power source.

The aluminum electrolysis cell (<NUM>) includes at least one an elongate vertical anode (<NUM>) extending upward from the upper surface (<NUM>) of the bottom. The elongate vertical anode (<NUM>) has a proximal end (<NUM>), a distal free end (<NUM>) and a middle portion (<NUM>). The proximal end (<NUM>) of the elongate vertical anode is connected to the upper surface (<NUM>) of the bottom. The distal free end (<NUM>) of the elongate vertical anode extends upward toward the refractory top cover (<NUM>). In some aspects , the elongate vertical anode (<NUM>) is aluminum-wettable. For example the elongate vertical anode (<NUM>) may comprise one or more of TiB2, ZrB2, HfB2, SrB2, carbonaceous material, W, Mo, and steel, and combinations thereof.

In some aspects , the aluminum electrolysis cell (<NUM>) includes a cathode connector (<NUM>) proximal the refractory top cover (<NUM>). The cathode connector (<NUM>) has an upper connection rod (<NUM>) and a lower surface (<NUM>). The upper connection rod (<NUM>) is configured to connect to the external power source.

The aluminum electrolysis cell (<NUM>) includes at least one elongate vertical cathode (<NUM>). The elongate vertical cathode (<NUM>) extends downward from the lower surface (<NUM>) of the cathode connector (<NUM>). The elongate vertical cathode (<NUM>) has a proximal end (<NUM>), a distal free end (<NUM>), and a middle portion (<NUM>). The proximal end (<NUM>) of the elongate vertical cathode is connected to the upper surface (<NUM>) of the cathode connector (<NUM>). The distal free end (<NUM>) of the vertical cathode extends downward toward the base (<NUM>) of the aluminum electrolysis cell. In some aspects , the elongate vertical cathode (<NUM>) is aluminum-wettable. For example the elongate vertical cathode (<NUM>) may comprise one or more of TiB2, ZrB2, HfB2, SrB2, carbonaceous material, and combinations thereof.

In the illustrated example of <FIG> and <FIG>, the elongate vertical cathode (<NUM>) overlaps the elongate vertical anode (<NUM>) such that the distal end (<NUM>) of the elongate vertical cathode (<NUM>) is proximal the middle portion (<NUM>) of the elongate vertical anode (<NUM>). Furthermore, in the illustrated embodiment, the distal end (<NUM>) of the elongate vertical anode (<NUM>) is proximal the middle portion (<NUM>) of the elongate vertical cathode (<NUM>). In some aspects , the anode-cathode overlap is configured to balance voltage requirements of the cell and/or energy consumption of the cell. In some embodiments, the anode-cathode overlap (ACO) is <NUM> to <NUM> inches. In some aspects , the anode-cathode overlap (ACO) is <NUM> to <NUM> inches. In some embodiments, the anode-cathode overlap (ACO) is <NUM> to <NUM> inches. In some aspects , the anode-cathode overlap (ACO) is <NUM> to <NUM> inches. In some aspects , the anode-cathode overlap (ACO) is <NUM> to <NUM> inches. In some aspects , the anode-cathode overlap (ACO) is <NUM> to <NUM> inches. In some aspects , the anode-cathode overlap (ACO) is at least some overlap up to <NUM> inches of overlap. In some aspects , the anode-cathode overlap (ACO) is at least <NUM> inches of overlap to <NUM> inches of overlap. In some aspects , the anode-cathode overlap (ACO) is at least <NUM> inches of overlap to <NUM> inches of overlap. In some aspects , the anode-cathode overlap (ACO) is at least <NUM> inches of overlap to <NUM> inches of overlap.

One or more inert spacers (<NUM>) may be located in between the elongate vertical cathode (<NUM>) from the elongate vertical anode (<NUM>) to maintain a desired anode to cathode distance (ACD). In some embodiments, the ACD may be <NUM>/<NUM> inch to <NUM> inches. In some embodiments, the ACD may be <NUM>/<NUM> inch to <NUM> inches. In some aspects , the ACD may be <NUM>/<NUM> inch to <NUM> inch. In some aspects , the ACD may be <NUM>/<NUM> inch to <NUM>/<NUM> inch. In some embodiments, the ACD may be <NUM>/<NUM> inch to <NUM>/<NUM> inch. In some aspects , the ACD may be <NUM>/<NUM> inch to <NUM>/<NUM> inch. In some aspects , the ACD may be <NUM>/<NUM> inch to <NUM> inch. In some aspects , the ACD may be <NUM>/<NUM> inch to <NUM>/<NUM> inch.

The refractory sidewalls (<NUM>), the refractory top cover (<NUM>), and the bottom (<NUM>) define a cell chamber (<NUM>) within the aluminum electrolysis cell (<NUM>). In some aspects , the cell chamber (<NUM>) contains: a molten metal pad (<NUM>), a top layer of purified molten aluminum (<NUM>), and an electrolyte (<NUM>). The molten metal pad (<NUM>) is in contact with the bottom (<NUM>). The electrolyte (<NUM>) separates the top layer (<NUM>) from the molten metal pad (<NUM>). The elongate vertical anode (<NUM>) extends upward from the bottom (<NUM>), through the molten metal pad (<NUM>) and terminates in the electrolyte (<NUM>). The elongate vertical cathode (<NUM>) extends downward from the cathode connector (<NUM>) and terminates in the electrolyte (<NUM>) such that the elongate vertical cathode (<NUM>) overlaps the elongate vertical anode (<NUM>) within the electrolyte (<NUM>). Thus, the elongate vertical cathode (<NUM>) is separated from the elongate vertical anode (<NUM>) by electrolyte (<NUM>).

As described above, the electrolyte (<NUM>) separates the top layer of purified aluminum (<NUM>) from the molten metal pad (<NUM>). In this regard, the composition of the electrolyte (<NUM>) may be selected such that the electrolyte (<NUM>) has a lower density than the molten metal pad (<NUM>) and higher density than the top layer of purified aluminum (<NUM>). In some aspects , the electrolyte (<NUM>) may comprise at least one of fluorides and/or chlorides of Na, K, Al, Ba, Ca, Ce, La, Cs, Rb, and combinations thereof, among others.

The molten metal pad (<NUM>) may comprise at least one alloy comprising one or more of Al, Si, Cu, Fe, Sb, Gd, Cd, Sn, Pb and impurities.

In some aspects , the purified molten aluminum has <NUM> wt. % to <NUM> wt. % aluminum. In some aspects , the purified molten aluminum has <NUM> wt. % to <NUM> wt. % aluminum. In some aspects , the purified molten aluminum has <NUM> wt. % to <NUM> wt. % aluminum. In some aspects , the purified molten aluminum has <NUM> wt. % to <NUM> wt. % aluminum. In some aspects , the purified molten aluminum has <NUM> wt. % to <NUM> wt. % aluminum. In some aspects , the purified molten aluminum has <NUM> wt. % to <NUM> wt. % aluminum. In some aspects , the purified molten aluminum has <NUM> wt. % to <NUM> wt. % aluminum.

In some aspects , the purified molten aluminum has <NUM> wt. % to <NUM> wt. % aluminum. In some aspects , the purified molten aluminum has <NUM> wt. % to <NUM> wt. % aluminum. In some aspects , the purified molten aluminum has <NUM> wt. % to <NUM> wt. % aluminum. In some aspects , the purified molten aluminum has <NUM> wt. % to <NUM> wt. % aluminum. In some aspects , the purified molten aluminum has <NUM> wt. % to <NUM> wt. % aluminum.

In some aspects , the aluminum electrolysis cell (<NUM>) includes a plurality of elongate vertical anodes (<NUM>). In some aspects , the aluminum electrolysis cell (<NUM>) includes a plurality of elongate vertical cathodes (<NUM>). The plurality of elongate vertical anodes (<NUM>) may be interleaved with the plurality of elongate vertical cathodes (<NUM>).

In some aspects , the aluminum electrolysis cell (<NUM>) includes a cell access channel (<NUM>) penetrating the cell chamber (<NUM>) thereby providing access to the lower portion of the cell chamber. The cell access channel (<NUM>) may have an access port (<NUM>). Aluminum feedstock (<NUM>) may be added to the aluminum electrolysis cell (<NUM>) via the access port (<NUM>).

In some aspects , the aluminum electrolysis cell (<NUM>) includes an aluminum extraction port (<NUM>) penetrating a refractory sidewall (<NUM>), thereby providing access to an upper portion of the cell chamber (<NUM>). Purified aluminum (<NUM>) may be extracted from the aluminum electrolysis cell (<NUM>) via the extraction port (<NUM>).

In some aspects , the aluminum electrolysis cell (<NUM>) includes an inert gas inlet formed in the refractory top cover (<NUM>). The inert gas inlet is configured to provide an inert atmosphere (<NUM>) to the cell chamber (<NUM>).

In some aspects , the aluminum electrolysis cell (<NUM>) includes an outer shell (<NUM>). The outer shell may comprise steel or other suitable materials. In some aspects , the outer shell (<NUM>) may include a shell floor (<NUM>) located beneath the base. In some aspects , the outer shell (<NUM>) may include shell sidewalls (<NUM>) spaced apart from and surrounding the refractory sidewalls (<NUM>).

In some aspects , the aluminum electrolysis cell (<NUM>) may include thermal insulation (<NUM>). The thermal may be located between the shell floor (<NUM>) and the base (<NUM>) and between the shell sidewalls (<NUM>) and the refractory sidewalls (<NUM>). The thermal insulation may facilitate high electrical efficiency of the aluminum electrolysis cell (<NUM>).

The inventive method for purifying aluminum includes supplying an electric current to the elongate vertical anode (<NUM>). Molten material, including molten aluminum, from the molten metal pad (<NUM>) may creep up the vertical surfaces of the elongate vertical anode (<NUM>). The upward creep of the molten material from the molten metal pad may occur continuously during operation of the cell (<NUM>). The molten material from the molten metal pad may cover essentially all of the exposed surfaces of the elongate vertical anode (<NUM>). The molten aluminum on the surface of the elongate vertical anode (<NUM>) may be anodized via the elongate vertical anode (<NUM>), thereby producing aluminum ions. At least some of the aluminum ions may be transported through the electrolyte onto the surface of the elongate vertical cathode (<NUM>). At least some of the aluminum ions may be reduced via the elongate vertical cathode (<NUM>), thereby producing purified aluminum on the surface of the elongate vertical cathode (<NUM>). Without being bound by a particular mechanism or theory, one possible explanation is that the purified aluminum then creep up the surface of the elongate vertical cathode (<NUM>) due to the buoyancy of the purified aluminum in the electrolyte (<NUM>). Thus, the purified aluminum may tend to collect as a layer (<NUM>) above the electrolyte (<NUM>). For example, based on differences in density between the purified aluminum product and the electrolyte (e.g. bath components in the electrolyte), and the molten metal pad (e.g. including feedstock with aluminum metal, impurities, and/or densifying aids (additives to increase density such that the metal pad is configured with a density greater than the electrolyte such that the molten metal pad zone is configured below the electrolyte zone.

The purified aluminum (<NUM>) may be produced via the electrolysis cell (<NUM>) at an energy efficiency of <NUM> to <NUM> kWh/kg of purified aluminum.

The purified aluminum (<NUM>) may be produced via the electrolysis cell (<NUM>) at an energy efficiency of <NUM> to <NUM> kWh/kg of purified aluminum. The purified aluminum (<NUM>) may be produced via the electrolysis cell (<NUM>) at an energy efficiency of <NUM> to <NUM> kWh/kg of purified aluminum. The purified aluminum (<NUM>) may be produced via the electrolysis cell (<NUM>) at an energy efficiency of <NUM> to <NUM> kWh/kg of purified aluminum. The purified aluminum (<NUM>) may be produced via the electrolysis cell (<NUM>) at an energy efficiency of <NUM> to <NUM> kWh/kg of purified aluminum.

The purified aluminum (<NUM>) may be produced via the electrolysis cell (<NUM>) at an energy efficiency of <NUM> to <NUM> kWh/kg of purified aluminum. The purified aluminum (<NUM>) may be produced via the electrolysis cell (<NUM>) at an energy efficiency of <NUM> to <NUM> kWh/kg of purified aluminum.

The method includes adding aluminum feedstock (<NUM>) into the cell chamber (<NUM>) via the cell access port (<NUM>). The aluminum feedstock (<NUM>) may be added essentially continuously during operation of the cell (<NUM>).

The aluminum feedstock (<NUM>) may be added by metering the aluminum feedstock (<NUM>) at a first feed rate. The aluminum feedstock (<NUM>) may be added periodically.

The method may include removing at least some of the top layer (<NUM>) of purified aluminum from the cell (<NUM>) via the aluminum extraction port (<NUM>).

The top layer (<NUM>) may be removed essentially continuously during operation of the cell (<NUM>). The first removal rate may be controlled, for example, based at least in part on the second removal rate. The top layer (<NUM>) may be removed periodically during operation of the cell (I).

The removing step is completed with equipment configured to remove the purified aluminum product without contaminating the product (e.g. alumina, graphite, and/or TiB2 tapping equipment).

The method may include providing an inert atmosphere to the cell chamber (<NUM>) via the inert gas inlet (<NUM>). In this regard, the cell chamber may be sealed from the ambient atmosphere. Examples of inert gases include helium, argon, and nitrogen, among others.

Sludge (<NUM>) may be produced due, at least in part, to the passing step. The sludge (<NUM>) may have a higher density than the molten metal pad (<NUM>). As described above, the upper surface (<NUM>) of the bottom (<NUM>) may be sloped.

The slope may run from a refractory sidewall (<NUM>) down towards the cell access channel (<NUM>). Thus, the sludge (<NUM>) may drain along the upper surface (<NUM>) towards the cell access channel (<NUM>). The sludge may be removed from the cell chamber (<NUM>) via the cell access channel (<NUM>). Impurities may tend to collect in the molten metal pad (<NUM>). Thus, the cell access channel (<NUM>) may facilitate removal of at least a portion of the molten metal pad (<NUM>).

The following examples are intended to illustrate the invention and should not be construed as limiting the invention in any way.

A schematic of the cell used to conduct lab trials of the electrolytic purification cell is shown in <FIG> and <FIG> (not to scale). <FIG> is a side schematic (elevation view) of the electrolytic purification cell used for bench scale trials. <FIG> is a top down schematic (plan view) of the electrolytic purification cell used for bench scale trials (the cathode assembly is not shown). <FIG> is a graph depicting experimental data obtained, illustrated as Fe in the metal, as determined through ICP (wt. %) depicted for each cell.

Four trial tests using different electrolytes and anode plate configurations were conducted using the cell configuration shown in the <FIG> and <FIG>. The cell was placed within an electric furnace (<NUM>) to heat and control cell temperature. Inside the furnace, the cell was contained in an Inconel retort (<NUM>) in which a graphite crucible (<NUM>) was placed. The graphite crucible provided the electrical connection to the anode aluminum pad at the bottom of the cell. An alumina liner (<NUM>) was placed within the graphite retort to provide electrical insulation between the graphite retort wall and the electrolyte, and the graphite retort wall and the cathode aluminum.

The impure aluminum (feed), alloyed with copper (e.g. as a densifying aid, at <NUM>-<NUM>%, targeted at <NUM>% by weight), was added to the cell as the anode aluminum. The copper was added to the impure aluminum to increase the melt density to be greater than the electrolyte. Two vertical anodes (TiB2 plates (<NUM>)) were installed in the anode aluminum pad with their ends extending vertically into the electrolyte.

The cathode electrical connection was constructed from a graphite block (<NUM>). A vertical cathode (TiB2 plate (<NUM>)) was pinned to the graphite cathode electrical connection and placed between the two anode plates. The cathode electrical connection was held by a superstructure not shown in <FIG>. The cathode plate had the same dimensions as each anode plate for trial <NUM>. For trial <NUM>, the anode plate area was doubled while the cathode plate area was the same as for trial <NUM>. The anode plate area was doubled by doubling its width where the width is the long dimension on the anode plate in the top down view of <FIG>. Two other runs, trial <NUM> and <NUM>, are depicted in Table <NUM>, with the results of all four trials depicted in <FIG>. The graphite block had a cavity to collect the pure aluminum as it was produced on the TiB2 plate and flowed upward due to buoyancy forces. The anode aluminum level (<NUM>) filled the bottom of the graphite crucible and decreased as the cell operated.

The electrolyte used in the trials was a mixture of AlF3, NaF, KF, and BaF2 salts. The electrolyte level (<NUM>) was maintained near the top of the graphite retort. The electrolyte mixture composition was chosen so that it had a density (when molten) between that of the anode aluminum and cathode aluminum. The electrolyte composition for trial <NUM> comprised BaF2, AlF3 and KF. The electrolyte composition for trial <NUM> comprised BaF2, AIF3 and NaF Other useful electrolyte compositions include those having at least <NUM>% BaF2 and at least <NUM>% AlF3.

The cell containing the anode aluminum alloy and electrolyte mixture was heated and maintained at a temperature of <NUM> to <NUM> degrees C by the electric furnace. A direct current of <NUM> to <NUM> amps was supplied between the anodes and cathode once the electrolyte mixture was at temperature.

Cell voltage, current and temperature were logged during each trial using a data acquisition system. Purified aluminum was collected in the cathode collection cavity. Iron impurity in the aluminum was measured to quantify purification performance from samples taken from the feed aluminum and purified molten aluminum. The elemental impurity concentrations from the molten aluminum were measured using inductively coupled plasma mass spectrometry (ICP).

The results from the two trials are shown in Table <NUM>, below.

Claim 1:
A method for purifying an aluminum feedstock comprising:
(a) feeding an aluminum feedstock into a cell access channel of an aluminum electrolysis cell, wherein the aluminum electrolysis cell comprises a molten metal pad zone and an electrolyte zone, and wherein the feeding comprises providing the aluminum feedstock to the molten metal pad zone;
(b) directing an electric current into an anode through an electrolyte and into a cathode, wherein the anode comprises an elongate vertical anode, and wherein the cathode comprises an elongate vertical cathode, wherein the anode and the cathode extend into the electrolyte zone, such that, within the electrolyte zone, the anode and cathode realize an anode-cathode overlap and an anode-cathode distance;
(c) wetting at least a portion of a surface of the elongate vertical anode with a molten material from the molten metal pad zone, the molten metal pad zone being a reservoir of molten material located below the electrolyte, wherein the molten material comprises aluminum metal;
(d) concomitant with the directing step, producing at least some aluminum ions in the electrolyte zone via the aluminum metal on the surface of the elongate vertical anode; and
(e) concomitant with the directing step, reducing at least some of the aluminum ions in the electrolyte zone at a surface of the elongate vertical cathode thereby producing a purified aluminum product.