Hollow fiber membrane, schematic

Fig. 5-10. Schematic representation of hollow-fiber membrane extraction.

Fig. 13.11 Schematic representation of the hollow fiber membrane biorector for the enzymatic hydrolysis of triglycerides. A hydrophilic membrane has been used, coated with lipase on the lipid side [85].

Figure 2. Schematic view of reverse osmosis test loop (I) hollow fiber membrane (2) pressure vessel (3) feed water (4) filter (5) pressure pump (6) relief valve.

Polymer-Assisted Ultrafiltration of Boric Acid. The Quickstand (AGT, Needham, MA) filtration apparatus is pictured schematically in Figure 3. The hollow fiber membrane module contained approximately 30 fibers with 0.5 mm internal diameter and had a nominal molecular weight cut-off of 10,000 and a surface area of 0.015 m2. A pinch clamp in the retentate recycle line was used to supply back pressure to the system. In a typical run, the transmembrane pressure was maintained at 25 psig and the retentate and permeate flow rates were 25 ml/min and 3 ml/min, respectively. Permeate flux remained constant throughout the experiments. 

Figure 3.32 Schematic of the principal types of hollow fiber membranes...

Another type of gas exchange process, developed to the pilot plant stage, is separation of gaseous olefin/paraffin mixtures by absorption of the olefin into silver nitrate solution. This process is related to the separation of olefin/paraffin mixtures by facilitated transport membranes described in Chapter 11. A membrane contactor provides a gas-liquid interface for gas absorption to take place a flow schematic of the process is shown in Figure 13.11 [28,29], The olefin/paraffin gas mixture is circulated on the outside of a hollow fiber membrane contactor, while a 1-5 M silver nitrate solution is circulated countercurrently down the fiber bores. Hydrophilic hollow fiber membranes, which are wetted by the aqueous silver nitrate solution, are used. 

FIGURE 33.9 Schematic view of hollow fiber membrane contactor operated in recycling mode for U(VI) recovery from aqueous acidic waste (1) HFC module, (2) feed, (3) extractant, and (4) peristaltic pumps. 

Based on the schematic diagram of the WGS hollow-fiber membrane reactor illustrated in Figure 9.1, the molar and energy balances were performed on both feed... 

Figure 9.1. Schematic diagram of water-gas shift hollow-fiber membrane reactor. (Reprinted with permission from Huang et al.,6 Copyright 2005 Elsevier.)...

Figure 9.10 Schematic diagram of vibrating hollow fiber membrane. From Ref. [136] with permission.

Figure 4.16. Schematic of a hollow-fiber EMB, 1 TCE polluted water, 2,9 peristaltic pumps, 3 hollow fibers membranes, 4 distribution tube, 5 baffle, 6 collection tube, 7 treated effluent, 8,14,16,17 sample ports, 10 lumen influent, 11 lumen effluent, 12 shell influent, 13 shell effluent, 15 plug flow reactor, 18 air, 19 methanol and nutrients, 20 waste, 21 growth chemostat. From Pressman et al. [4.138], with permission from John Wiley Sons Inc.

Figure 1.33 Schematic diagram showing membrane modules presently used in industrial separation processes (a) pleated membrane filter cartridge (b) plate-and-frame membrane module (c) spiral wound membrane module (d) tubular membrane module (e) capillary membrane module (f) hollow fiber membrane module.

We have developed a one-dimensional non-isothermal model for the countercurrent WGS membrane reactor with a C02-selective membrane in the hollow-fiber configuration using air as the sweep gas. Figure 1 shows the schematic of each hollow-fiber membrane with catalyst particles in the reactor. The modeling study of the membrane reactor is based on (1) the CO2 / H2 selectivity and CO2 permeance reported by Ho [1, 2] and (2) low-temperature WGS reaction kinetics for the commercial catalyst copper oxide, zinc oxide, aluminum oxide (CuO/ZnO/ AI2O3) reported by Moe [3] and others [4]. In this modeling study, the model that we have developed has taken into account critical system parameters including temperature, pressure, feed gas flow rate, sweep gas (air) flow rate, CO2 permeance, CO2 /H2 selectivity, CO concentration, CO conversion, H2 purity, H2 recovery, CO2 concentration, membrane area, water (H20)/C0 ratio, and reaction equilibrium. 

FIGURE 5.70 Schematic of a hollow-fiber membrane cartridge used for blood dialysis. 

FIGURE 10.36 Schematics of different vibration strategies for submerged hollow fiber membranes, (a) Vertical vibration, (b) transverse vibration, and (c) liquid oscillation. 

In the simulation of the HMD process, the gas-permeation membrane used is assumed to be an asymmetric hollow-fiber membrane. For this type of membrane, gas permeation does not depend on the flow pattern on the permeate side as the porous supporting layer prevents mixing of the permeate fluxes (Pan, 1986). A schematic of the flow pattern in an asymmetric hollow-fiber membrane is shown in Figure 10.2. Hence, a simple cross-flow model is sufficient to describe the membrane behavior. 

Figure 10.2 Schematic of the flow pattern in an asymmetric hollow-fiber membrane.

Fig. 14.4.1.2. Schematic diagram of a two-phase hollow-fiber membrane bioreactor system for hydrolytic epoxide resolution. [After reference 8]. The yeast cells contain an epoxide hydrolase that enantioselectively hydrolyzes racemic epoxide resulting in enantiopure epoxide that partitions to the organic phase. Diol produced partitions to the water phase.

A schematic diagram of the polymer precipitation process is shown in Figure 7. The hot polymer solution is cast onto a water-cooled chill roll, which cools the solution, causing the polymer to precipitate. The precipitated film is passed through an extraction tank containing methanol, ethanol, or isopropanol to remove the solvent. Finally, the membrane is dried, sent to a laser inspection station, trimmed and rolled up. The process shown in Figure 7 is used to make fiat-sheet membranes. The preparation of hollow-fiber membranes by the same general technique has also been described. 

Figure 10.22 Schematic diagrams of the hollow fiber membrane interface (a) and the CIEF-IMER-nanoRPLCMS platform (b) [131]. Source Copyright 2011 Wiley-VCH Veriag GmbH, Weinheim.

Figure 8.1.35. Schematic of various large-scale liquid-liquid extraction devices, (a) Packed tower for solvent extraction (b) sieve-plate extraction column (c) an early Scheibel column extraction design (d) Karr column, in which the plates have reciprocating motions (e) centrifugal extractor (f) porous hollow fiber membrane solvent extraction device (see Figure 8.1.13(a) for a detailed design).

The process of dialysis, in which small solutes diffuse from a feed solution through a microporous membrane into the dialyzing solution, was illustrated in Section 4.3.1 via a membrane kept in a closed vessel To achieve separation in a continuous fashion, we realized there that the dialyzer had to be open. Such a device is schematically shown in Figure 8.1.46(a). A small hollow fiber membrane based dialyzer used as an artificial kidney is illustrated in Figure 8.1.46(b). Both utilize countercurrent flow of feed solution (for example, blood) and the dialyzing solution on two sides of the membrane. 

Figure 1.16 Schematic diagram of the hollow fiber membrane reactor. Reproduced with permission from [16], Copyright (2013), Woodhead Publishing (Elsevier).

Figure 8.5 Schematic diagram of the catalytic hollow fiber membrane (a) flow pattern (b) catalyst coated on inner surface [5] (c) catalyst impregnated inside the wall. Reproduced from [30]. With permission from Elsevier.

Perstraction is possible with hollow fiber membranes in order to achieve a higher surface area [63], but may also be subject to clogging (Table 10.4) [64]. Interestingly, pervaporation is potentially one of the most attractive methods, although the volatility of the product is clearly of great importance. A comprehensive comparison of methods should also indicate the cost as well as the benefit of any flow sheet modification, relative to a base case as schematically shown in Figure 10.3. 

The hollow fiber membrane module assembles a shell-and-tube heat exchanger. It consists of a large number of hollow fibers assembled in a module, as shown schematically in Figure 5.8. The free ends of the fibers are potted with agents such as epoxy resins, polyurethanes, silicone rubber, thermoplastics, thermosets or inorganic cements. In some cases they can also be fused by heating. 

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