Filtration flux

A continuous cross-flow filtration process has been utilized to investigate the effectiveness in the separation of nano sized (3-5 nm) iron-based catalyst particles from simulated Fischer-Tropsch (FT) catalyst/wax slurry in a pilot-scale slurry bubble column reactor (SBCR). A prototype stainless steel cross-flow filtration module (nominal pore opening of 0.1 pm) was used. A series of cross-flow filtration experiments were initiated to study the effect of mono-olefins and aliphatic alcohol on the filtration flux and membrane performance. 1-hexadecene and 1-dodecanol were doped into activated iron catalyst slurry (with Polywax 500 and 655 as simulated FT wax) to evaluate the effect of their presence on filtration performance. The 1-hexadecene concentrations were varied from 5 to 25 wt% and 1-dodecanol concentrations were varied from 6 to 17 wt% to simulate a range of FT reactor slurries reported in literature. The addition of 1-dodecanol was found to decrease the permeation rate, while the addition of 1-hexadecene was found to have an insignificant or no effect on the permeation rate. 

As part of a downstream processing sequence, 10 m3 of a process fluid containing 20 kg m 3 of an enzyme is to be concentrated to 200 kg/m3 by means of ultrafiltration. Tests have shown that the enzyme is completely retained by a 10,000 MWCO surface-modified polysulphone membrane with a filtration flux given by ... 

Figure 8.2 Filtrate flux versus TMP in ultrafiltration of serum solutions.

The following empirical dimensional equation [5], which is based on data for the UF of diluted blood plasma, can correlate the filtrate flux/p (cm min ) averaged over the hollow fiber of length/, (cm) ... 

Equation 8.7 [6] was obtained to correlate the experimental data on membrane plasmapheresis, which is the MF of blood to separate the blood cells from the plasma. The filtrate flux is affected by the blood velocity along the membrane. Since, in plasmapheresis, all of the protein molecules and other solutes will pass into the filtrate, the concentration polarization of protein molecules is inconceivable. In fact, the hydraulic pressure difference in plasmapheresis is smaller than that in the UF of plasma. Thus, the concentration polarization of red blood cells was assumed in deriving Equation 8.7. The shape of the red blood cell is approximately discoid, with a concave area at the central portion, the cells being approximately 1-2.5 pm thick and 7-8.5 pm in diameter. Thus, a value of r (= 0.000257 cm), the radius of the sphere with a volume equal to that of a red blood cell, was used in Equation 8.7. 

Here, /p is the filtrate flux (cm min ) averaged over the hollow fiber membrane of length L (cm) and is the shear rate (s ) on the membrane surface, as in Equation 8.6. The volumetric percentage of red blood cells (the hematocrit) was taken as C, and its value on the membrane surface, Cg, was assumed to be 95%. 

Blood cells are separated from blood (hematocrit 40%) by microfiltration, using hollow-fiber membranes with an inside diameter of 300 pm and a length of 20 cm. The average flow rate of blood is 5.5 cm s T Estimate the filtrate flux. 

The apparent reflection coefficient (=(C5g - C pf/C, centration of solute in the permeate) may depend on the filtrate flux, when the real reflection coefficient cr is constant. Explain the possible reason for this. 

Albumin solutions (1, 2, and 5wt%) are continuously ultrafiltered through a flat plate filter with a channel height of 2 mm. Under cross-flow filtration with a transmembrane pressure of 0.5 MPa, steady-state filtrate fluxes (cm min ) are obtained as given in Table P9.2. 

As stated in Chapter 9, cross-flow filtration (CFF) provides a higher efficiency than dead-end filtration, as some of particles retained on the membrane surface are swept off by the liquid flowing parallel to the surface. As shown by a solid line in Figure 14.6 [3], filtrate flux decreases with time from the start of filtration due to an accumulation of filtered particles on the membrane surface, as in the case of dead-end filtration. The flux then reaches an almost constant value, where... 

Figure 14.6 Cross-flow filtration flux of baker s yeast suspension. Cell concentration 7%. Transmembrane pressure 0.49 bar. Flow rate 0.5 ms". ...

Ihe estimation of a steady-state value of the CFF filtrate flux in general is... 

This balance of forces on the approach of particles to membrane pores also has substantial consequences for rates of filtration. Of special interest is the case where the particle to be removed is comparable to or only slightly greater in dimensions than the pore diameter. In the absence of colloidal interactions, this can lead in a catastrophic loss in filtration flux as such particles can plug pores highly effectively. Such a fouling mechan-... 

Fig. 14.6. Filtration flux as a function of time of filtration for the filtration of O.Oi g/L silica particles in 0.001 M NaCI solution at pH 6 at a membrane of mean pore diameter 84 nm. The particle size was very close to the pore size. The critical transmembrane pressure for these conditions was calculated as 130 kPa. Operation below this pressure gives only a gradual decline in filtration flux with time. Operation above this pressure gives an initially higher filtration flux which declines rapidly with time. In the latter case the intial hydrodynamic force exceeds the electrical double layer repulsion between the membrane and the particles, causing the particles to block the membrane pores.

Filtration. Filtration can include filter presses, rotary drum vacuum filters (RDVF), belt filters, and variations on synthetic membrane filtration equipment, such as filter cartridges, pancake filters, or plate and frame filter presses. These processes typically operate in a batch mode when the filter chamber is filled up or the vacuum drum cake is exhausted, a new batch must be started. This type of filtration is also called dead-end filtration because the only fluid flow is through the membrane itself. Due to the small size of cells and their compressible nature, typical cell cakes have low permeability and filter aids, such as diatomaceous earths, perlite, or other mined materials are added to overcome this limitation. Moreover, the presence of high solids and viscous polymeric fermentation byproducts can limit filtration fluxes without the use of filter aids. 

Fungal fermentations, such as those of Trichoderma or Aspergillus sp., lend themselves particularly well to cell separation by filtration through a rotary drum vacuum filter because of the ease with which the fungal mat can be shaved off by the drum s knife, renewing the filter cake surface to maintain high filtration flux. 

Surface water can also be processed to become drinking water but it requires some pretreatment prior to the microfiltration step. A filtrate flux of 1,000-1,500 L/hr-m can be realized [Guibaud, 1989]. 

Microriltraticiii and ultraTiltratiop of lees or crude wines. More specifically, crossflow micro- and ultra-filtration ceramic membranes have the potential for replacing all the above separation steps except cold treatment [Castelas and Serrano, 1989]. When using inorganic membranes for removing bacterias, yeasts or suspended particles, the choice of the pore size is very important in determining the filtrate flux and the rejection performance of these materials from wines. 

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