Water holdup

Viswanathan et al. (V6) measured gas holdup in fluidized beds of quartz particles of 0.649- and 0.928-mm mean diameter and glass beads of 4-mm diameter. The fluid media were air and water. Holdup measurements were also carried out for air-water systems free of solids in order to evaluate the influence of the solid particles. It was found that the gas holdup of a bed of 4-mm particles was higher than that of a solids-free system, whereas the gas holdup in a bed of 0.649- or 0.928-mm particles was lower than that of a solids-free system. An attempt was made to correlate the gas holdup data for gas-liquid fluidized beds using a mathematical model for two-phase gas-liquid systems proposed by Bankoff (B4). 

For example, the small tolerance and low surface roughness of the plate in manufacture are critical for assuring the high electrical contact conductivity, low fluid flow resistance, and low water holdup to meet performance require-menfs of fhe plates. Moreover, to play the role of removing generated water in the cathode side—particularly to avoid flooding when fhe current density is high, the surface of the cathode plate may need hydrophobicity [11] so as to better adjust hydrophobic and hydrophilic properties of plate materials in cathode and anode plates. This area needs further study. 

Holdup and start-up time. McWilliams and co-workers [M4] have found that the holdup of Spraypak no. 37 under these conditions is about 41b water/ft, or 0.064 g/cm . Consequently, the total water holdup of the columns of a plant producing 1 g-mol of DjO/s would be (0.064X1.02 X 10")/18 = 3.63 X 10 g-mol water. From Eqs. (13.17), (12.199), and (12.203), the average deuterium content of the water inventory of this plant is... 

One possible difficulty with Fig. 13.21 is the much higher average deuterium content of water in the electrolytic cells compared with Fig. 13.20. This requires that cell leak rates and water holdup be kept small. 

The water holdup should be sufficient to provide a 10-foot slug of water in the inlet line to the drum if an explosion occurs downstream of the drum. 

ISSUE TITLE Diversion of recirculation water (holdups in containment) (SS 5)... 

Liquid surface tension has practically no effect on operating holdup for high surface tension liquids, such as water. For ordinary organic liquids (a about 27 dyne/cm) at low liquid rates, the operating holdup will be about 12% lower than for water. Holdup will be reduced up to 20%, for low surface tension systems (a about 13 dyne/cm) at low liquid rates. At liquid rates above 7 gpm/ft this effect of surface tension on liquid holdup diminishes. These measurements were determined at atmospheric pressure and should not be extrapolated to high-pressure distillations. 

The eomplete leakage process is clearly illustrated in Figure 3 that shows a series of snapshots of water (completion brine) holdup profiles (green eurves) prior to and shortly after the leakage. For this ease, a water holdup less than 1 at a well depth means that there is CO2 present at the specific location. 

Simply put, water holdup is defined as the fraetion of water occupied cross-section area over a total cross-section area. Water holdup of 1 is equivaloit to 100% water in the cross-section, whereas water holdup of 0 means no water in the cross-section. 

To prevent such release, off gases are treated in Charcoal Delay Systems, which delay the release of xenon and krypton, and other radioactive gases, such as iodine and methyl iodide, until sufficient time has elapsed for the short-Hved radioactivity to decay. The delay time is increased by increasing the mass of adsorbent and by lowering the temperature and humidity for a boiling water reactor (BWR), a typical system containing 211 of activated carbon operated at 255 K, at 500 K dewpoint, and 101 kPa (15 psia) would provide about 42 days holdup for xenon and 1.8 days holdup for krypton (88). Humidity reduction is typically provided by a combination of a cooler-condenser and a molecular sieve adsorbent bed. 

Gas flow in these rotary dryers may be cocurrent or countercurrent. Cocurrent operation is preferred for heat-sensitive materials because gas and product leave at the same temperature. Countercurrent operation allows a product temperature higher than the exit gas temperature and dryer efficiency may be as high as 70%. Some dryers have enlarged cylinder sections at the material exit end to increase material holdup, reduce gas velocity, and minimize dusting. Indirectly heated tubes are installed in some dryers for additional heating capacity. To prevent dust and vapor escape at the cylinder seals, most rotary dryers operate at a negative internal pressure of 50—100 Pa (0.5—1.0 cm of water). 

In order to cool to the equilibrium temperature, a pond of infinite size would be required for warm water. An approach of 1.7 to 2.2°C (3 to 4°F) is the lowest practicable in a pond of reasonable size. For a pond having more than a 24-h holdup, the leaving-water temperature will vary from the average by plus or minus 1.1°C (2°F) for a 0.9-m (5-ft) depth and 1.7°C (3°F) variation for a 0.9-m (3-ft) depth. 

FIG. 14-58 Typical holdup data for random packings and the air-water system. The raschig rings are of ceramic material. To convert pounds per hour per fr to Idlograms per second per m , multiply hy 0.001.356 to convert inches to millimeters, miinltiplyhy 25.4. [Shulman etal., AIChE J. i, 247 (I.9.5.5).]... 

FIG. 14-60 Comp arison of measured and calculated values of liquid holdup for Gempak 2A structured packing, air-water system. [Rocha et al., Ind. Eng. Chem., 32, 641 (1.9.93).] Reproduced with permission. Copyright 199.3 American Chemical Society. 

The difference between the curves for pure water and seawater again illustrates the significance of small concentrations of solute with respecl to bubble behavior. In commercial bubble columns and agitated vessels coalescence and breakup are so rapid and violent that the rise velocity of a single bubble is meaningless. The average rise velocity can, however, be readily calculated from holdup correlations that will be given later. 

Direction of extraction, whether from dispersed to continuous, organic hquid to water, or the reverse Dispersed-phase holdup Flow rates and flow ratio of the liquids... 

Bubble sizes tend to a minimum regardless of power input because coalescence eventually sets in. Pure liquids are coalescing type solutions with electrolytes are noncoalescing but their bubbles also tend to a minimum. Agitated bubble size in air/water is about 0..5 mm (0.020 in), holdup fractions are about 0.10 coalescing and 0.2.5 noncoalescing, but more elaborate correlations have been made. 

The heat of reaction requires cooling water at the rate of 10 to 40 L/(1,000 L holdup)(h). Vessels under about 500 L (17.6 fF) are provided with jackets, larger ones with coils. For a 55,000-L vessel, 50 to 70 m" maybe taken as average. 

For vaporAiquid separators there is often a liquid residence (holdup) time required for process surge. Tables 1, 2, and 3 give various rules of thumb for approximate work. The vessel design method in this chapter under the Vapor/Liquid Calculation Method heading blends the required liquid surge with the required vapor space to obtain the total separator volume. Finally, a check is made to see if the provided liquid surge allow s time for any entrained water to settle. 

Piret et al. measured liquid holdup in a column of 2J-ft diameter and 6-ft packed height, packed with graded round gravel of lj-in. size, the total voidage of the bed being 38.8%. The fluid media, air and water, were in countercurrent flow. The liquid holdup was found to increase markedly with liquid flow rate, but was independent of gas flow rate below the loading point. Above the loading point, an increase of liquid hold-up with gas flow rate was observed. 

Ross (R2) measured liquid-phase holdup and residence-time distribution by a tracer-pulse technique. Experiments were carried out for cocurrent flow in model columns of 2- and 4-in. diameter with air and water as fluid media, as well as in pilot-scale and industrial-scale reactors of 2-in. and 6.5-ft diameters used for the catalytic hydrogenation of petroleum fractions. The columns were packed with commercial cylindrical catalyst pellets of -in. diameter and length. The liquid holdup was from 40 to 50% of total bed volume for nominal liquid velocities from 8 to 200 ft/hr in the model reactors, from 26 to 32% of volume for nominal liquid velocities from 6 to 10.5 ft/hr in the pilot unit, and from 20 to 27 % for nominal liquid velocities from 27.9 to 68.6 ft/hr in the industrial unit. In that work, a few sets of results of residence-time distribution experiments are reported in graphical form, as tracer-response curves. 

Hoogendoorn and Lips (H10) carried out residence-time distribution experiments for countercurrent trickle flow in a column of 1.33-ft diameter and 5- and 10-ft height packed with -in. porcelain Raschig rings. The fluid media were air and water, and ammonium chloride was used as tracer. The total liquid holdup was calculated from the mean residence time as found... 

Larkins et al. (L2) visually observed flow patterns and measured pressure drop and liquid holdup for cocurrent downflow of gas and liquid through beds of spheres, cylinders, and Raschig rings of diameters from 3 mm to f in. in experimental columns of 2- and 4-in. diameter, as well as in a commercial unit several feet in diameter. The fluid media were air, carbon dioxide, or natural gas and water, water containing methylcellulose, water containing soap, ethylene glycol, kerosene, lubricating oil, or hexane. 

Measurements for water containing 0.2% ethanol, the addition of which was found to influence markedly the gas holdup (see Section V,B,3), indicate that variation of surface tension has no significant effect upon axial mixing. The results for 2-mm spheres could not be correlated by a similar expression. It is proposed in that work that the flow mechanism in this case is significantly different because of the higher ratio between bubble size and particle size. 

Verschoor (V5) studied the motion of swarms of gas bubbles formed at a porous glass gas distributor. Gas holdup was observed to increase approximately linearly with nominal gas velocity up to a critical point (corresponding to a nominal gas velocity of about 4 cm/sec), whereupon it decreased to a minimum and then increased again on further increase of the gas velocity. Higher holdup was observed for a water-glycerine mixture than for water. 

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