Electrochemical plating cell having a membrane stack
Embodiments of the invention generally provide an electrochemical plating cell having cell body defining a fluid containing region, an anode positioned in the fluid containing region, and a membrane stack positioned across the fluid containing region at a position above the anode and below a substrate receiving opening formed into the cell body. The membrane stack includes an ionic membrane, a first membrane stack positioned on an upper surface of the ionic membrane, and a second membrane stack position on a lower surface of the ionic membrane.
This application claims benefit of U.S. provisional patent application Ser. No. 60/515,464, filed Oct. 29, 2003, which is herein incorporated by reference.
BACKGROUND OF THE INVENTION1. Field of the Invention
Embodiments of the present invention generally relate to a membrane stack for a plating cell that may be used adjacent and anode of the cell or positioned spaced from the anode between the anode and a substrate being plated.
2. Description of the Related Art
Metallization of sub 100 nanometer features is a foundational technology for present and future generations of integrated circuit manufacturing processes. More particularly, in devices such as ultra large scale integration-type devices, i.e., devices having integrated circuits with more than a million logic gates, the multilevel interconnects that lie at the heart of these devices are generally formed by filling high aspect ratio, i.e., greater than about 15:1, interconnect features with a conductive material, such as copper. Conventional deposition techniques, such as chemical vapor deposition (CVD) and physical vapor deposition (PVD) have been unsuccessful in filling features of this size, and as such, plating techniques, i.e., electrochemical plating (ECP) and electroless plating, have emerged as promising processes for void free filling of sub 100 nanometer sized high aspect ratio interconnect features in integrated circuit manufacturing processes.
Conventional electrochemical plating cells have recently been modified to include a fluid impermeable membrane is positioned to separate the fluid basin of the cell into an anode compartment and a cathode compartment. However, since the membrane is positioned between the anode of the plating cell and the substrate being plated, the material being plated onto the substrate generally passes through the membrane. This passage of copper, for example, has been shown to create boundary layers on both the top and bottom sides of the membrane, which are undesirable for controlling plating parameters and defect ratios. As such, there is a need for a plating cell configured to eliminate the challenges associated with generating boundary layers on the separation membrane surfaces.
SUMMARY OF THE INVENTIONEmbodiments of the invention provide an electrochemical plating cell. The plating cell includes a fluid basin having a fluid inlet and a fluid outlet, an ionic membrane sealably positioned across the fluid basin to separate the fluid basin into a catholyte and anolyte volume, an anode positioned in the anolyte volume, a first membrane stack positioned on a first side of the ionic membrane, and a second membrane stack positioned on a second side of the ionic membrane.
Embodiments of the invention generally provide an electrochemical plating cell. The cell includes cell body defining a fluid containing region, an anode positioned in the fluid containing region, and a membrane stack positioned across the fluid containing region at a position above the anode and below a substrate receiving opening formed into the cell body. The membrane stack includes an ionic membrane, a first membrane stack positioned on an upper surface of the ionic membrane, and a second membrane stack position on a lower surface of the ionic membrane.
Embodiments of the invention generally provide an electrochemical plating cell having a membrane stack therein. The plating cell includes a fluid basin having a fluid inlet and a fluid outlet configured to receive a substrate, an anode position in the fluid basin, and a cationic membrane positioned across the fluid basin. The plating cell further includes a first membrane positioned over the cationic membrane and having a pore diameter of between about 2 um and about 20 um, a second membrane positioned over the first membrane and having a pore diameter of between about 0.1 um and about 15 um, a third membrane positioned under the cationic membrane and having a pore diameter of between about 2 um and about 20 um, a fourth membrane positioned under the third membrane and having a pore diameter of between about 0.1 um and about 15 um, a first fluid outlet in fluid communication with a fluid volume between the first membrane and the cationic membrane, and a second fluid outlet in fluid communication with a fluid volume between the ionic membrane and the third membrane.
BRIEF DESCRIPTION OF THE DRAWINGSSo that the manner in which the above recited features of the present invention can be understood in detail, a more particular description of the invention, briefly summarized above, may be had by reference to embodiments, some of which are illustrated in the appended drawings. It is to be noted, however, that the appended drawings illustrate only typical embodiments of this invention and are therefore not to be considered limiting of its scope, for the invention may admit to other equally effective embodiments.
The processing mainframe 113 includes a substrate transfer robot 120 centrally positioned thereon. Robot 120 generally includes one or more arms/blades 122, 124 configured to support and transfer substrates thereon. Additionally, the robot 120 and the accompanying blades 122, 124 are generally configured to extend, rotate, and vertically move so that the robot 120 may insert and remove substrates to and from a plurality of processing locations 102, 104, 106, 108, 110, 112, 114, 116 positioned on the mainframe 113. Similarly, factory interface robot 132 also includes the ability to rotate, extend, and vertically move its substrate support blade(s), while also allowing for linear travel along the robot track that extends from the factory interface 130 to the mainframe 113. Generally, process locations 102, 104, 106, 108, 110, 112, 114, 116 may be any number of processing cells utilized in an electrochemical plating platform. More particularly, the process locations may be configured as electrochemical plating cells, rinsing cells, bevel clean cells, spin rinse dry cells, substrate surface cleaning cells (which collectively includes cleaning, rinsing, etching, and ozone treatment cells, etc.), electroless plating cells, metrology inspection stations, and/or other processing cells that may be beneficially used in conjunction with a plating platform. Each of the respective processing cells and robots are generally in communication with a process controller 111, which may be a microprocessor-based control system configured to receive inputs from both a user and/or various sensors positioned on the system 100 and appropriately control the operation of system 100 in accordance with the inputs.
In the exemplary plating system 100 illustrated in
Plating cell 200 is generally positioned at a tilt angle, i.e., a frame portion 203 of plating cell 200 is generally elevated on one side such that the components of plating cell 200 are tilted between about 3° and about 30° from horizontal, or generally between about 4° and about 10°. The frame member 203 of plating cell 200 supports an annular base member 204 on an upper portion thereof, and since frame member 203 is elevated on one side, the upper surface of base member 204 is generally tilted from the horizontal at an angle that corresponds to the tilt angle of frame member 203 relative to a horizontal position. However, embodiments of the invention are not limited to tilted plating cells, as positioning the plating cell 200 at any angle with respect to horizontal, including 0°, for example, is contemplated within the scope of the invention.
Base member 204 generally includes an annular or disk shaped recess formed into a central portion thereof, the annular recess being configured to receive a disk shaped anode member 205 therein. Base member 204 further includes a plurality of fluid inlets/drains 209 extending from a lower surface thereof. Each of the fluid inlets/drains 209 are generally configured to individually supply or drain a fluid to or from either the anode compartment or the cathode compartment of plating cell 200 via conduits (not shown) formed through the base member 204. Anode member 205 generally includes a plurality of slots 207 formed therethrough, wherein the slots 207 are generally positioned in parallel orientation with each other across the surface of the anode 205. The parallel orientation allows for dense fluids generated at the anode surface to flow downwardly across the anode surface and into one of the slots 207. However, embodiments of the invention are not limited to slotted-type anodes, as various other anodes, including solid disk-type anodes and other anodes conventionally used in electrochemical plating, are contemplated within the scope of the invention.
Plating cell 200 further includes a membrane support assembly 206. Membrane support assembly 206 is generally secured at an outer periphery thereof to base member 204, and includes an interior region configured to allow fluids to pass therethrough. A membrane 208 is stretched across the support 206 and generally operates to fluidly separate a catholyte chamber (positioned adjacent the substrate being plated) and anolyte chamber (positioned adjacent the anode electrode in the cell) of the plating cell. The membrane support assembly 206 may include an o-ring type seal positioned near a perimeter of the membrane 208, wherein the seal is configured to prevent fluids from traveling from one side of the membrane 208 secured on the membrane support 206 to the other side of the membrane 208. As such, membrane 208 generally provides fluid isolation between the anode and cathode portions of the plating cell 200, i.e., via use of a cationic membrane. Exemplary membranes that may be used to fluidly isolate an anolyte from a catholyte are illustrated in commonly assigned U.S. patent application Ser. No. 10/627,336 filed on Jul. 24, 2003 entitled “Electrochemical Processing Cell”, which is hereby incorporated by reference in its entirety. Alternatively, membrane 208 may be a fluid permeable filter-type membrane that allows fluid to pass therethrough.
A diffusion plate 210, which is generally a porous ceramic disk member or other fluid permeable electrically resistive member is positioned in the cell between anode 205 and the membrane 208. The positioning of the diffusion member 210 below the membrane 208 is a departure from conventional plating cells where the diffusion member would generally be positioned above the membrane 208 adjacent the substrate being plated. When the diffusion member 210 is placed below the membrane 208, it does not generate substantially laminar flow of electrolyte toward the plating surface, as with conventional plating cells having the diffusion member above the membrane. The inventors have concluded that a substantially laminar flow may not be necessary, as the plating thickness or uniformity is predominantly controlled by the electric field and boundary layer thickness, and not the fluid flow at the plating surface, as previously thought. The boundary layer thickness at the substrate is driven mostly by the relative motion of the wafer and fluid induced by rotation of the substrate during the plating process. Put simply, the inventors profess that the uniformity of a plating process is affected by the electric field primarily, then the rotationally induced boundary layer, then the vertical flow induced boundary layer, in that order. As such, by the time variations in the vertical fluid flow are considered, the impact on the uniformity is a third or even fourth order effect.
However, there still is a benefit to a implementing a diffuser in a plating cell. That benefit is that it increases the cell electrical impedance, and in doing so, reduces the percentage increase in the cell voltage as the soluble anode erodes, and in effect, moves away from the substrate. To this end, if the diffuser thickness is doubled, the uniformity decreases with a single “standard” thickness, and if it is taken away, the uniformity, except at the very edge, improves. The edge effect is E-field driven, which is fixed by other techniques. In the case of this invention, the diffuser has the additional task of compensating for the difference in anolyte and catholyte conductivities, the path length for which is varying as a result of the tilt in the membrane relative to the workpiece. Further still, positioning the diffuser in the catholyte serves as a bubble trap, which has been shown to contribute to undesirable plating defects.
With the diffuser 210 positioned below the membrane 208, the diffusion member 210 is positioned in the anolyte solution, i.e., the solution flowing below the membrane 208 that does not include plating additives and that does not contact the plating surface of the substrate being plated. The diffusion member 210 is generally manufactured from an electrically insulating material, and as such, the diffusion member 210 also operates to control the electric field generated between the anode and the substrate. In conventional plating cells, and in some embodiments of the invention, the diffusion member 210 is a disk shaped member having a uniform thickness across the surface thereof.
However, in plating cell configurations wherein the upper surface of the anode 205 and the surface of the membrane 208 are not positioned in parallel relationship with each other, as will be further discussed herein, the diffusion member 210 may be configured to have a varying thickness across the surface thereof. More particularly, the thickness of the diffusion member 210 may be varied to compensate for variances in the resistance path between the anode 205 and the substrate being plated, such that the perpendicular line resistance between the anode 205 and the substrate being plated remains constant across all points on the surface of the substrate. Additionally, with regard to the type of the diffusion member 210 described above, embodiments of the invention are not intended to be limited to ceramic diffusion members, as other electrically insulative fluid permeable (porous) materials that are non-reactive with electrochemical processing fluids may also be used in embodiments of the invention without departing from the scope thereof. Additionally, embodiments of the invention further contemplate that electrically insulative materials that are not porous may also be used in embodiments of the invention, i.e., as holes or bores may be formed through the electrically insulative material to allow fluid to flow therethrough in a manner similar to the fluid flow through the above noted porous diffusion member.
When a porous diffusion member is implemented in embodiments of the invention, then the porosity of the diffusion member 210 may be between about 20% and about 60%, and more particularly, between about 30% and about 50%. These porosities have been shown to generate a resistivity when wet with electrolyte that is between about three and ten times greater or higher than the resistivity of the same shape of cell without the diffusion member 210 positioned therein. The thickness of the diffusion member 210 may be between about 1 mm and about 30 mm, for example, for a disk shaped or uniform thickness diffusion member 210, which has also shown improved plating characteristics when plating material onto thin seed layers, i.e., seed layers having a thickness of less than about 500 Å.
Further, positioning of the diffusion member 210 in the anolyte solution, e.g., below the membrane 208, assists with minimizing bubbles present at the substrate surface and removes the diffusion member as a possible source for surface defects on the substrate. Additional advantages of positioning the diffusion member 210 in the anolyte include improved terminal effect results and an improved ability to counteract the local variations in the resistivity of the membrane 208 and the anode 205. The positioning of the diffusion member 210 between the membrane 208 and the anode 205 also allows for the plating cell to be positioned vertically instead of tilted, which may mitigate immersion defects.
Additional embodiments of the exemplary plating cell illustrated in
In the embodiment of the invention illustrated in
The embodiment of the invention illustrated in
Further, embodiments of the invention, and in particular, the embodiments of the invention illustrated in
In another embodiment of the invention, which is illustrated in the general sectional view of
The ionic membrane 408 is generally a cationic membrane configured to allow positively charged ions, such as Cu2+ to travel upward through the membrane 408 from the anode 405 to the substrate being plated, while preventing plating solution additives and other constituents from traveling downward through the membrane from the catholyte solution into the anolyte solution where they may contact the anode 405 and breakdown. Exemplary ionic membranes that may be used in embodiments of the invention are described in commonly assigned U.S. patent application Ser. No. 10/616,044 filed on Jul. 8, 2003 entitled “Anolyte for Copper Plating”, which is hereby incorporated by reference in its entirety.
The first membrane stack 420 generally includes a first membrane 421 positioned adjacent the ionic membrane 408 and a second membrane 422 positioned above the first membrane 421, such that the first membrane 421 is positioned between the second membrane 422 and the ionic membrane 408. The first membrane 421 is generally a hydrophilic fluid permeable membrane having a thickness of between about 50 μm and about 150 μm and having pores sized (diameter) between about 2 μm and about 20 μm, for example. The first membrane 421 is generally positioned immediately above the ionic membrane 408 with only a minimal fluid passage space positioned between the two membranes. The second membrane 422 is generally positioned immediately above the first membrane 421, again with a fluid passage space separating the membranes. The second membrane 422 generally has a thickness of between about 30 μm and about 175 μm and includes pores sized between about 0.1 μm and about 15 μm, for example. The outer perimeter of the first and second membranes 421, 422 is sealably attached to a sidewall 401 of the plating cell 400. The fluid space between the ionic membrane 408 and the first membrane 421 includes a catholyte fluid drain 425 positioned in communication therewith, while the fluid space positioned between the first and second membranes 421, 422 is sealably in communication with the sidewall 401 of the cell 400. The catholyte fluid drain 425 is also in fluid communication with a catholyte region 461 of the plating cell 400. Further, a corresponding catholyte supply 463 is in fluid communication with the catholyte region 461.
The second membrane stack 422 (positioned on the lower surface of the ionic membrane 408) also includes a two layer membrane stack. The membrane stack includes a first membrane 427 positioned adjacent the ionic membrane 408 and a second membrane 428 positioned adjacent the first membrane 427, such that the first membrane 427 is positioned between the second membrane 428 and the ionic membrane 408. Both the first and second membranes 427, 428 are sealably attached to the sidewall 401 of the plating cell 400. Further, first membrane 427 is positioned such that there is a fluid space positioned between the ionic membrane 408 and the first membrane 427. Similarly, the second membrane 428 is positioned such that there is a fluid space between the second membrane 428 and the first membrane 427. The fluid space between the ionic membrane 408 and the first membrane 427 is in fluid communication with an anolyte drain 426. The first membrane 427 is generally a hydrophilic fluid permeable membrane having a thickness of between about 50 μm and about 150 μm and having pores sized (diameter) between about 2 μm and about 20 μm, for example. The second membrane 427 generally has a thickness of between about 30 μm and about 175 μm and includes pores sized between about 1 μm and about 15 μm, for example.
The third membrane stack 440 is positioned on the upper surface of the anode 405. The third membrane stack generally includes a first membrane 441 and a second membrane 442. The first membrane 441 is generally positioned next to the upper surface of the anode 405, with a fluid space separating the anode 405 from the membrane 441. The second membrane 442 is positioned above the first membrane 441 and is separated from the first membrane 441 by a fluid space. Both the first and second membranes 441, 442 are generally sealably attached to the sidewall 401 of the plating cell 400, however, the fluid space between the first membrane 441 and the anode 405 includes an anolyte drain 428 positioned in fluid communication therewith. The anolyte drain 428 is also generally in fluid communication with an anolyte region 460 of the plating cell 400. Further, an anolyte supply line 462 is in fluid communication with the anolyte region 460.
In operation, the embodiment of the invention illustrated in
In this embodiment the copper ions in the anolyte solution are transferred through the diffusion member 210 and through the membrane 208 toward the substrate being plated during the electrolytic plating process. However, plating additives and contaminants that may accumulate in the catholyte solution are not permitted by virtue of the cationic membrane properties that do not allow these constituents to pass through the membrane 208 in the direction of the anode. The perpendicular line resistance between the anode 205 and the substrate being plated (which is generally positioned parallel to the anode during plating) is generally constant at all points across the anode 205, and further, as a result of the positioning of the diffusion member 210 in the anolyte, the resistance is substantially higher than in conventional plating cells.
In the embodiment of the invention illustrated in
The operational characteristics of the embodiment of the invention illustrated in
The second membrane stack 430 operates in a similar manner to the first membrane stack 420. More particularly, a first large porous membrane 427 is positioned adjacent a lower surface of the ionic membrane 408 and a second smaller porous membrane 428 is positioned adjacent the first membrane 427. The anolyte drain 428 operates to remove anolyte from the fluid volume between the lower surface of the ionic membrane 408 and the first membrane 427, which again generates a reduced pressure that pulls replacement fluid into the volume. The replacement fluid, i.e., anolyte, is pulled from through the second membrane 428 and first membrane 427 into the fluid volume between the first membrane 427 and the lower surface of the ionic membrane 408. This configuration generally operates to circulate the anolyte solution that is depleted of copper ions, i.e., the anolyte solution adjacent the ionic membrane surface, away from the surface of the ionic membrane 408. This provides a continual and sufficient supply of copper ions for transport through the ionic membrane 408, which in turn operates to prevent the cell voltage from rising as a result of a copper ion deficiency at the ionic membrane 408.
The third membrane stack 440 provides a similar function to the anode 405 as membrane stacks 420, 430 do for the ionic membrane 408. More particularly, the positioning of the larger porous first membrane 441 adjacent the anode and the smaller porous second membrane 442 adjacent the first porous membrane 441 operates to flush material away from the surface of the anode 405. Specifically, the anolyte conduit 426 is in fluid communication with the fluid volume between the first membrane 441 and the anode 405 and is configured to remove anolyte therefrom. As such, a negative pressure is generated in the fluid volume between the first membrane 441 and the anode 405, which operates to pull anolyte into the fluid volume. The anolyte being pulled into the fluid volume travels through the second membrane 442 and the first membrane 441 to reach the fluid volume, and is then removed therefrom by the anolyte conduit 426, thus generating an anolyte circulation loop. The larger porous membrane 441 is similar in construction, thickness, and pore size to the first membrane 421 of first stack 420, and the second membrane 442 is similar in construction, thickness, and pore size to the second membrane 422 of the first membrane stack 420.
The third membrane stack 440 generally operates to pull sludge that forms on the surface of the anode away from the anode surface, which reduces the need to tilt the plating cell in order to urge the sludge to flow into the anode slots for removal from the anode surface. Additionally, this flow pattern also operates to pull the copper rich anolyte away from the anode surface and circulate the copper rich anolyte into the bulk anolyte solution volume, which allows higher plating rates that do not require increased fluid flow in the plating cell. Additional benefits of the third membrane stack 440 positioned on or immediately above the anode 405 include reduced anode passiviation at current densities of less than about 80 mA/cm2, reduced bowing of the ionic membrane 408 as a result of increased fluid pressure, which also minimizes center thin plating challenges, elimination of metallization of the ionic membrane 408, and increased anode life, as a slotted anode configuration, such as the anode 205 illustrated in
While the foregoing is directed to embodiments of the present invention, other and further embodiments of the invention may be devised without departing from the basic scope thereof, wherein the scope thereof is determined by the claims that follow.
Claims
1. An electrochemical plating cell, comprising:
- a fluid basin having a fluid inlet and a fluid outlet;
- an ionic membrane sealably positioned across the fluid basin to separate the fluid basin into a catholyte volume and an anolyte volume;
- an anode positioned in the anolyte volume;
- a first membrane stack positioned on a first side of the ionic membrane; and
- a second membrane stack positioned on a second side of the ionic membrane.
2. The plating cell of claim 1, wherein the first membrane stack comprises:
- a first membrane positioned adjacent the ionic membrane, the first membrane having a thickness of between about 50 um and about 150 um; and
- a second membrane positioned adjacent the first membrane and between the first membrane and a substrate being plated, the second membrane having a thickness of between about 30 um and about 175 um.
3. The plating cell of claim 2, wherein first membrane has a pore diameter of between about 2 um and about 20 um.
4. The plating cell of claim 2, wherein the second membrane has a pore diameter of between about 0.1 um and about 15 um.
5. The plating cell of claim 4, wherein the first membrane has a pore diameter of between about 2 um and about 20 um.
6. The plating cell of claim 1, wherein the second membrane stack comprises a third membrane positioned adjacent the second side of the ionic membrane and a fourth membrane positioned between the third membrane and the anode.
7. The plating cell of claim 6, wherein the third membrane has a pore diameter of between about 2 um and about 20 um.
8. The plating cell of claim 6, wherein the fourth membrane has a pore diameter of between about 0.1 um and about 15 um.
9. The plating cell of claim 8, wherein the third membrane has a pore diameter of between about 2 um and about 20 um.
10. The plating cell of claim 6, further comprising an anolyte drain in fluid communication with a fluid volume positioned between the second side of the ionic membrane and the third membrane.
11. The plating cell of claim 6, further comprising a catholyte drain in fluid communication with a fluid volume positioned between the first side of the ionic membrane and the first membrane.
12. The plating cell of claim 1, further comprising a third membrane stack positioned on an upper surface of the anode, the third membrane stack comprising a fifth membrane positioned adjacent the upper surface and a sixth membrane positioned above the fifth membrane.
13. The plating cell of claim 12, wherein the fifth membrane has a pore diameter of between about 2 um and about 20 um.
14. The plating cell of claim 13, wherein the sixth membrane has a pore diameter of between about 0.1 um and about 15 um.
15. The plating cell of claim 13, wherein the sixth membrane has a pore diameter of between about 0.1 um and about 15 um.
16. An electrochemical plating cell, comprising:
- a cell body defining a fluid containing region;
- an anode positioned in the fluid containing region; and
- a membrane stack positioned across the fluid containing region at a position above the anode and below a substrate receiving opening formed into the cell body, the membrane stack comprising: an ionic membrane; a first membrane stack positioned on an upper surface of the ionic membrane; and a second membrane stack position on a lower surface of the ionic membrane.
17. The plating cell of claim 16, where the first membrane stack comprises:
- a first membrane positioned next to the upper surface, the first membrane having a pore diameter of between about 2 um and about 20 um; and
- a second membrane positioned adjacent the first membrane and between the first membrane and a substrate being plated, the second membrane having a pore diameter of between about 0.1 um and about 15 um.
18. The plating cell of claim 16, wherein the second membrane stack comprises a third membrane positioned adjacent the lower surface of the ionic membrane and having a pore diameter of between about 2 um and about 20 um, and a fourth membrane positioned between the third membrane and the anode and having a pore diameter of between about 0.1 um and about 15 um.
19. The plating cell of claim 16, further comprising an anolyte drain in fluid communication with a fluid volume positioned between the lower side of the ionic membrane and the third membrane.
20. The plating cell of claim 16, further comprising a catholyte drain in fluid communication with a fluid volume positioned between the upper side of the ionic membrane and the first membrane.
21. The plating cell of claim 16, further comprising a third membrane stack positioned on an upper surface of the anode, the third membrane stack comprising a fifth membrane positioned adjacent the upper surface and a sixth membrane positioned above the fifth membrane.
22. The plating cell of claim 21, wherein the fifth membrane has a pore diameter of between about 2 um and about 20 um and the sixth membrane has a pore diameter of between about 0.1 um and about 15 um.
23. An electrochemical plating cell, comprising:
- a fluid basin having a fluid inlet and a fluid outlet configured to receive a substrate;
- an anode position in the fluid basin;
- a cationic membrane positioned across the fluid basin;
- a first membrane positioned over the cationic membrane and having a pore diameter of between about 2 um and about 20 um;
- a second membrane positioned over the first membrane and having a pore diameter of between about 0.1 um and about 15 um;
- a third membrane positioned under the cationic membrane and having a pore diameter of between about 2 um and about 20 um;
- a fourth membrane positioned under the third membrane and having a pore diameter of between about 0.1 um and about 15 um;
- a first fluid outlet in fluid communication with a fluid volume between the first membrane and the cationic membrane; and
- a second fluid outlet in fluid communication with a fluid volume between the ionic membrane and the third membrane.
24. The plating cell of claim 23, wherein the ionic membrane is positioned at a tilt angle.
25. The plating cell of claim 23, further comprising:
- a fifth membrane positioned on an upper surface of the anode, the fifth membrane having a pore diameter of between about 2 um and about 20 um; and
- a sixth membrane positioned over the fifth membrane and having a pore diameter of between about 0.1 um and about 15 um.
26. The plating cell of claim 25, further comprising a fluid drain in communication with a fluid volume between the upper surface of the anode and the fifth membrane.
Type: Application
Filed: Aug 26, 2004
Publication Date: May 5, 2005
Inventor: Harald Herchen (Los Altos, CA)
Application Number: 10/927,367