Membrane separation application

Porous glass structures have not been marketed for membrane separation applications until recently, despite having been studied as a membrane material for a long time. A number of glass companies such as Asahi Glass... 

Membrane processes can be operated in two major modes according to the direction of the feed stream relative to the orientation of the membrane surface dead-end filtration and crossflow filtration (Figure 1.1). The majority of the membrane separation applications use the concept of crossflow where the feed flows parallel to and past the membrane surface while the permeate penetrates through the membrane overall in a... 

Although most of the discussions on backflushing so far use the crossflow configuration as an example, backflushing also can be and has been employed in through-flow membrane separation applications. 

As in many other membrane separation applications, the clean water flux is essentially proportional to the transmembrane pressure difference (TMP). When solutes, macromolecules or particulates are to be separated from the solvent (e.g., water), the permeate flux is first a linear function of the TMP and is in the pressure controlled regime. Although similar to the behavior of water flux, the permeate flux is nevertheless lower. Beyond a "threshold pressure," the permeate flux is insensitive to TMP due to concentration and gel polarization near the membrane surface. This behavior is so-called mass transfer controlled. It appears that the larger pore membrane, 50 nm in pore diameter, reaches the threshold pressure sooner than the finer pore membrane, 4 nm in pore diameter. There is a significant advantage of operating the membranes at a higher... 

In cross-flow filtration (Fig. IB), shear forces are introduced at the cake surface to reduce cake thickness and total cake resistance. It is exclusively used in membrane separation applications to prevent fouling on membranes. 

Studies of these perfluorinated membranes in dilute and in concentrated solution environments still leave many unanswered questions about the nature of membrane transport properties. However, the obvious importance of these polymers in membrane separation applications, coupled with the fundamental significance of their ion clustered morphology, makes the continued study of these materials a fruitful area of research for the future. 

PAI exhibit interesting properties for membrane separation applications. Both permeability and selectivity may be enhanced by the incorporation of bulky pendent groups. Such groups make the molecular structure rigid and keep voids. In comparison to Pis, PAI membranes can be more easily fabricated. 

Membrane separation applications with higher selectivity, capacity, and flow rates are driven by the need for more economical and robust manufacturing processes providing higher-purity products. In the area of virus and sterile filtration, membrane providers are developing high-capacity and high-flux membranes by the use of multilayer structures. 

Many membrane separation applications have already benefitted from membrane modification strategies. Chapter 10 describes how bespoke polymeric membranes have been used to improve the crystallization of biomolecules. Membrane crystallization allows through a careful control of the process parameters the production of crystals with controlled shape, size, size distribution, and polymorphism. Further research is required to provide comprehensive understanding of the complex relationships between membrane process parameters and crystal structure. The control of product polymorphism will continue to be important in the pharmaceutical industry, which, as the range of drugs and their specificity increase, will reqnire improved... 

Cross-flow-elec trofiltratiou (CF-EF) is the multifunctional separation process which combines the electrophoretic migration present in elec trofiltration with the particle diffusion and radial-migration forces present in cross-flow filtration (CFF) (microfiltration includes cross-flow filtration as one mode of operation in Membrane Separation Processes which appears later in this section) in order to reduce further the formation of filter cake. Cross-flow-electrofiltratiou can even eliminate the formation of filter cake entirely. This process should find application in the filtration of suspensions when there are charged particles as well as a relatively low conduc tivity in the continuous phase. Low conductivity in the continuous phase is necessary in order to minimize the amount of elec trical power necessaiy to sustain the elec tric field. Low-ionic-strength aqueous media and nonaqueous suspending media fulfill this requirement. 

Advantages to Membrane Separation This subsertion covers the commercially important membrane applications. AU except electrodialysis are pressure driven. All except pervaporation involve no phase change. All tend to be inherently low-energy consumers in the-oiy if not in practice. They operate by a different mechanism than do other separation methods, so they have a unique profile of strengths and weaknesses. In some cases they provide unusual sharpness of separation, but in most cases they perform a separation at lower cost, provide more valuable products, and do so with fewer undesirable side effects than older separations methods. The membrane interposes a new phase between feed and product. It controls the transfer of mass between feed and product. It is a kinetic, not an equihbrium process. In a separation, a membrane will be selective because it passes some components much more rapidly than others. Many membranes are veiy selective. Membrane separations are often simpler than the alternatives. 

Plate-and-Frame (Conceptually the simplest, it is veiv much like a filter press. Once found in RO, UF, and IVIF, it is still the only module commonly used in electrodialysis (ED). A fevy applications in pressure-driven membrane separation remain (see Sec. 18 for a description of a plate-and-frarne filter press). 

Refinery product separation falls into a number of common classes namely Main fractionators gas plants classical distillation, extraction (liquid-liquid), precipitation (solvent deasphalting), solid facilitated (Parex(TM), PSA), and Membrane (PRSIM(TM)). This list has been ordered from most common to least common. Main fractionators are required in every refinery. Nearly every refinery has some type of gas plant. Most refineries have classical distillation columns. Liquid-liquid extraction is in a few places. Precipitation, solid facilitated and membrane separations are used in specific applications. 

Most of the chiral membrane-assisted applications can be considered as a modality of liquid-liquid extraction, and will be discussed in the next section. However, it is worth mentioning here a device developed by Keurentjes et al., in which two miscible chiral liquids with opposing enantiomers of the chiral selector flow counter-currently through a column, separated by a nonmiscible liquid membrane [179]. In this case the selector molecules are located out of the liquid membrane and both enantiomers are needed. The system allows recovery of the two enantiomers of the racemic mixture to be separated. Thus, using dihexyltartrate and poly(lactic acid), the authors described the resolution of different drugs, such as norephedrine, salbu-tamol, terbutaline, ibuprofen or propranolol. 

J. T. F. Keurentjes, F. J. M. Voermans, Membrane separations in the production of optically pure compounds in Chirality and Industry II. Developments in the Manufacture and applications of optically active compounds, A. N. Collins, G. N. Sheldrake, J. Crosby (Eds.), John Wiley Sons, New York (1997) Chapter 8. 

L. J. Brice, W. H. Pirkle, Enantioselective transport through liquid membranes in Chiral separations, applications and technology, S. Ahuja (Ed.), American Chemical Society, Washington... 

In this chapter we will provide an overview of the application of membrane separations for chiral resolutions. As we will focus on physical separations, the use of membranes in kinetic (bio)resolutions will not be discussed. This chapter is intended to provide an impression, though not exhaustive, of the status of the development of membrane processes for chiral separations. The different options will be discussed on the basis of their applicability on a large scale. 

Armstrong and Jin [15] reported the separation of several hydrophobic isomers (including (l-ferrocenylethyl)thiophenol, 1 -benzylnornicotine, mephenytoin and disopyramide) by cyclodextrins as chiral selectors. A wide variety of crown ethers have been synthesized for application in enantioselective liquid membrane separation, such as binaphthyl-, biphenanthryl-, helicene-, tetrahydrofuran and cyclohex-anediol-based crown ethers [16-20]. Brice and Pirkle [7] give a comprehensive overview of the characteristics and performance of the various crown ethers used as chiral selectors in liquid membrane separation. 

Possible applications of MIP membranes are in the field of sensor systems and separation technology. With respect to MIP membrane-based sensors, selective ligand binding to the membrane or selective permeation through the membrane can be used for the generation of a specific signal. Practical chiral separation by MIP membranes still faces reproducibility problems in the preparation methods, as well as mass transfer limitations inside the membrane. To overcome mass transfer limitations, MIP nanoparticles embedded in liquid membranes could be an alternative approach to develop chiral membrane separation by molecular imprinting [44]. 

As described above, the application of classical liquid- liquid extractions often results in extreme flow ratios. To avoid this, a completely symmetrical system has been developed at Akzo Nobel in the early 1990s [64, 65]. In this system, a supported liquid-membrane separates two miscible chiral liquids containing opposite chiral selectors (Fig. 5-13). When the two liquids flow countercurrently, any desired degree of separation can be achieved. As a result of the system being symmetrical, the racemic mixture to be separated must be added in the middle. Due to the fact that enantioselectivity usually is more pronounced in a nonaqueous environment, organic liquids are used as the chiral liquids and the membrane liquid is aqueous. In this case the chiral selector molecules are lipophilic in order to avoid transport across the liquid membrane. 

A limitation to the more widespread use of membrane separation processes is membrane fouling, as would be expected in the industrial application of such finely porous materials. Fouling results in a continuous decline in membrane penneation rate, an increased rejection of low molecular weight solutes and eventually blocking of flow channels. On start-up of a process, a reduction in membrane permeation rate to 30-10% of the pure water permeation rate after a few minutes of operation is common for ultrafiltration. Such a rapid decrease may be even more extreme for microfiltration. This is often followed by a more gradual... 

New results of multiple membrane separation are presented, which showed a possible feasibility for industrial application in the near future The NF permeate obtained (membrane NF90) could meet specifications for water reuse in the textile industry... 

Basic technology for membrane separation of biomolecules was invented in the United States, but the West Germans and the Japanese lead in its application to separations of enzymes and amino acids from complex mixtures. Japanese... 

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