Frequently Asked Questions

Yes, our Bi-Planar Feed Spacer Mesh is extruded from FDA compliant polypropylene.

We have a Chemical Compatibility Chart that you can use for reference.

Please refer to the following diagram to examine recommended feed flow rates for the crossflow cell you are working with.

Q: What is the pore size for the sintered stainless steel membrane support in the CF016 and CF042 test cells?

A: The pore size of the sintered stainless steel membrane support is approximately 20 microns.

For supported crossflow membranes, the membrane active side (smooth side) should be facing the feed stream and the support side (rough side) should be facing the permeate stream. For the Sterlitech Sepa CF, CF042, and CF016 test cells, the membrane side (smooth side) would face down toward the feed stream.

Yes, you may attempt to reuse flat sheet membranes. However, you may find it difficult to achieve a leak free seal. The cell body o-rings necessarily compress the membrane during installation and the physical action of separating the membrane from the o-rings during removal may cause damage. This damage can impede that ability to achieve a leak free seal when the membrane is reused.

No, you cannot use a foulant spacer that is thicker than the test cell feed channel as it may cause damage to the membrane.

Yes, you can use a foulant spacer that is thinner than the test cell feed channel. To do so, you should install a shim, or combination of shims, in the bottom of the feed channel below the foulant spacer so that the combined thickness of the shim(s) and foulant spacer is equal to, or slight less than, the depth of the feed channel.

The Sterlitech bench-scale crossflow test cells are available in a variety of materials to suit most applications:

• Stainless Steel
• PTFE
• Hastelloy^TM
• Delrin (natural acetal copolymer)
• Acrylic

Addtionally, there are a variety of available o-ring seals including Buna-N, EPDM, Viton, FEP encapsulated Viton, and FFKM (Markez).

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Cross flow velocity is calculated by dividing the volumetric flow rate through the cell by the cross section area of the cell. 

Cross flow velocity affects the hydrodynamic conditions in the system and therefore affects the rate of fouling. If the objective of the experiment is to mimic the hydrodynamic conditions in commercially available spiral wound elements it is recommended to stay in the range recommended by the manufacturers. Please contact Sterlitech for more information. 

If the objective of the experiment is to shed light into the effect of cross flow velocity on the membrane performance/fouling, the optimum range of cross flow velocity should be identified experimentally.

Q: What are the torque settings for the CF042 and Sepa CF Cells?

A: Best practices for plumbing of polymer (Acrylic, Delrin, and PTFE cells) CF042 cells, include the use of PTFE tape properly installed on 1/4npt threaded coupling, and the use of a light coat of PTFE-based pipe thread sealant, then the coupling needs to be seated in the base of the cell using the following torque settings:

• Delrin- 60 inch pounds
• Acrylic -70 inch pounds
• PTFE -15 inch pounds OR until the fitting "shoulders" out on the base of the CF042 cell*

*extreme caution should be used to assure that the fitting is not started incorrectly (cross-threaded).  In normal installation, the fitting should easily turn in several turns without tooling (by "hand") before using the torque wrench.

Mobil DTE 24 hydraulic oil or equivalent.

Q. Is there a difference in membrane rejection and permeate flux for a crossflow test cell operated continuously versus being operated in intervals?

A. Yes, there may be a difference in membrane rejection and permeate flux, at least initially during the operating intervals. At startup, there is a period of membrane conditioning that occurs as a result of mechanical compression.

This conditioning influences the rejection and permeate flux and is to some extent reversible when the operating pressure is relieved.

Consequently, there is a period of membrane conditioning that occurs every time the system is restarted. For sufficiently long operating intervals, the rejection and permeate flux will approach those for continuous operation.

GFD is an abbreviation for gallons per square foot per day. It is a common unit of measure for membrane permeate flow.

Most separations and flux through membranes are controlled by the nature of the fluid. For salt rejecting membranes (RO and NF), the dominant variables are operating pressure and osmotic pressure (a solute concentration-dependent property which reduces net operating pressure with increased solute concentrate).

Generally, permeate flux increases as the operating pressure increases; however, due to physical limitations of membranes, there is a practical limit above which increasing the operating pressure provides little or no flux increase. The fluid velocity across the membrane, controlled by the feed pump rate and concentrate control valve, is another important operating parameter. As the fluid velocity increases, the amount of mixing of the feed solution in the fluid layer directly above the membrane surface increases. The removal of fluid through the membrane (permeate) results in accumulation of rejected solutes in this layer, referred to as the boundary layer.

The accumulation of solutes in the boundary layer can contribute a significant resistance to permeate flux through the membrane and is often the factor most limiting permeate flux. Increasing the feed solution velocity across the membrane and using turbulence promoting foulant spacers, provides the optimal combination for boundary layer mixing to mitigate solute accumulation. However, considerations of energy expenditures and mechanical stress limitations of the membrane and the test cell system result in practical limitations for crossflow velocity. To find maximum permeate flux, we set the feed flow (and consequently the crossflow velocity) to a maximum practical rate and increase the operating pressure incrementally while monitoring the flux output.

Typically, a given operating pressure can be found that will yield maximum permeate flux specific to the feed solution and feed flow. If the feed is recirculated and the solute concentration changes, then the optimal operating pressure may change and typically decreases as solute concentration increases unless the osmotic pressure becomes significant. For systems operated with recirculating feed, it may be more optimal to operate at a pressure somewhat lower than the maximum pressure initially determined and may result in greater total permeate flux over time.

Q. Can I operate a crossflow test cell without a foulant spacer?

A. Depending on the feed pressure and crossflow velocity, operating a crossflow test cell without a foulant spacer may cause the membrane to become wrinkled and damaged, and is not recommended.

Typically, a foulant spacer with the same thickness as the feed channel is used. A foulant spacer thinner than the feed channel can be used in combination with a shim (or shims) of appropriate thickness.

Q. Could the filter cloth of industrial filters be used in the Sepa filtrations units, after cutting it to proper size?

A. The Sepa CF can potentially work for any media that can be fitted into the chamber.

One thing that could be an issue for some types of filter media is whether or not a sufficient seal is made between the O-ring and the media. For membranes, this is not a problem because membranes have a relatively smooth surface, which affords good mechanical seal when pressed together. A large fiber woven material, for example, may need to be modified or filled with some type of potting compound to level the surface in order to get a non-bypass seal.

Q. In the instruction manual for the Sepa CF, mesh and tubular foulant spacers are mentioned. What is the difference?

A. The 31 mil low foulant spacer and the 47mil medium foulant spacer have a mesh design with discrete openings.

The 65mil high foulant spacer has a tubular or corrugated, design without discrete openings.

The tubular design is less likely to be fouled by feed streams with elevated particle loading.

Q. Is the 17mil low foulant spacer the same as the 17mil permeate carrier?  Can the permeate carrier be used as a foulant spacer?

A. No, the foulant spacer and the permeate carrier are not the same. The foulant spacer is designed to accommodate particulate in the feed stream and to enhance the crossflow action near the membrane surface. Since there is essentially no particulate in the permeate stream, the permeate carrier is optimized to provide maximum support to the membrane without concern for accommodating particulate. Consequently, the permeate carrier should not be used as a foulant spacer.

Q. How do I distinguish between the low foulant (34ml) feed spacer and the high foulant (68ml) feed spacer when I hold them in my hands?

A. The low foulant has smaller squares and bends slightly easier.  It feels lighter.  It is not stiff like the medium foulant.  The high foulant spacer has corragated ridges in it like cardboard.  No holes.

The Reynolds number is a dimensionless number that is related to the ratio of inertial forces to viscous forces experienced by a fluid for given flow conditions. The Reynolds number can be used to predict whether flow conditions result in a laminar or turbulent flow.

In theory, the cross section area of the test cell feed channel can be used to calculate the Reynolds number for the feed flow. In practice, it is very difficult to calculate the Reynolds number because of the complex geometry of the foulant spacer occupying the feed channel. There are empirical methods to estimate the Reynolds number by characterizing the relationship between feed flow and differential pressure.

Please contact us at [email protected] if you need assistance.

It is not uncommon for the foulant spacer to leave an imprint on the membrane and, in most cases, is not a cause for concern.

However, it is important to verify that the foulant spacer (or the foulant spacer and shim combination) is not thicker than the feed channel. If too thick of a foulant spacer is used, then it may cause damage to the membrane.

 Passivation is a process that removes free iron deposits from stainless steel surfaces and, consequently, enhances corrosion resistance. To passivate a stainless steel test cell, generously swab all stainless surfaces (both external and internal) with either a 20% nitric acid solution (best choice) or 20% phosphoric acid solution (if more readily available). Allow the acid solution to sit for several minutes and then thoroughly rinse off with purified water.

Make sure to use proper precautions and wear necessary personal protective equipment (PPE) throughout this process. Passivation is only appropriate for stainless steel and must not be attempted on other materials; in particular, do not apply acids to the aluminum cell holder of the Sepa CF.