Brine flush

The injection of polymer solution was started after the brine permeability measurements. At a constant flow rate (6 ft/d) several pore volumes of polymer solution were injected through a sandpack. After the polymer flow cycle, the water lines before the sand face were flushed out with brine, and the injection of brine was initiated. During polymer flow and brine flush the injection pressures were recorded. Liquid samples were taken during both flow cycles. The polymer concentrations were determined from the radioactivities of the liquid samples. 

After brine flush the sandholders were taken apart. Two sand samples were taken at 1 cm and 6 cm distances from the injection face. The retained polymer in the sand samples was determined via radioactivity. 

After the polymer injection, a few pore volumes of brine were injected through the sandpack. The pressure during brine flush was again recorded. 

The first member of the right hand side of Equation (1) represents the distribution of retained polymer due to mechanical entrapment. The second member is constant, and the value of it depends on whether Equation (1) is applied for steady-state polymer flow or after sufficient brine flush to establish residual polymer retention. 

Equation (1) can also be applied to describe the retained polymer after brine flush. The meaning of the first member on the right-hand side of Equation (1) is the same as during polymer flow. The C , member, however, has a different meaning. It also consists of two parts. The first part originates from the physical adsorption in... 

The second part of during brine flush originates from the mechanical entrapment at inflnite distance, and the value of it is the same as during polymer flow. 

To summarize the thoughts above, values of C , are given below for polymer flow and brine flush. 

The treated core was then subjected to a large bank of brine and the pressure increased threefold during the subsequent 150 feet (2000 PV) of polymer injection. The treatment with hexylammonium ion must have been removed partially from the core during the brine flush. Next, the hexylammonium ions, bonded on the rock surface of the treated" core, were completely removed by a 1.5% sodium hypochlorite solution and another large bank of fresh brine. Consequently, the pressure increased sixfold at 250 ft (3300 PV) of polymer injection, as shown in Figure 10. After complete removal of the organic cation treatment from the core, the polymer plugging of the treated core was very similar to that of the untreated cores. 

An apparent negative inaccessible displaceable volume was obtained for several cores when the brine-flush portion of the flow test was evaluated using Eq. 1. The three cores exhibiting this behavior (Cores 42, 48, and 73, Table 2) ate of sufficiently low permeability that a substantial fraction of the pores could have diameters smaller than nominal polymer-molecule dimensions in solution.This could cause plugging of the tighter pores, with trapping of subsequent flowing polymer. Release of... 

To a flask flushed with nitrogen is added 0.06 mmol of telrakis(triphcnylphosphane)palladium, 2 mmol of (Z)-/ -bromoslyrene, 12 mL of THF and 3 mmol of a solution of the zinc reagent 19B in THF. After stirring for 3 h at 50 CC, the reaction mixture is diluted with 50 mL of benzene, washed quickly with brine and dried over MgS()4. Concentration and bulb-to-bulb distillation (bath 65-70 °C, 0.05 Torr)gives 3as a viscous oil yield 68%. 

Procedure. Core floods were carried out in horizontally mounted Berea sandstone cores of length 61 cm and diameter 5 cm. Porosity varied from 18 to 25% and brine permeability from 100 to 800 Jim2. The cores were coated with a thin layer of epoxy and cast in stainless steel core holders using molten Cerrobend alloy (melting point 70°C). The ends of the cores were machined flush with the core holder and flanges were bolted on. Pore volume was determined by vacuum followed by imbibition of brine. Absolute permeability and porosity were determined. The cores were initially saturated with brine (2% NaCl). An oil flood was then started at a rate of lOm/day until an irreducible water saturation (26-38%) was established. 

Salinity of seawater captured by various sampling devices in the CEPEX enclosure indicates problems not revealed in the usual oceanographic sampling situation. Relative to peristaltic pumping, all samples exhibited some salinity anomalies. Inadequate flushing to rinse the sampler of any concentrated brine or entrapped seawater is thought to be a problem. 

Impurities in the brine cause deposits to gradually accumulate on the cell base-plate. As a result the cell must occasionally be flushed out and then put back on-line. When the cell is adjusted after a cleaning process the objective is to start-up with a particular... 

Bis(l,2-ditellurolo)naphtacenef Tellurium powder (7.65 g, 60 mmol), 1.38 g (60 mmol) of sodium and 100 mL of dry dimethylformamide are placed in an argon-flushed flask fitted with a magnetic stirrer. The mixture is stirred and heated at 100°C for 1 h and then cooled to 55°C whereupon 5.0 g (14 mmol) of 5,6,11,12-tetrachlorononaphthacene followed by 100 mL of dimethylformamide are added. The resultant mixture is heated at 50°C for 20 h, poured into brine and filtered. The solid is dried, extracted with acetone and benzene and the solid is recrystallized from chlorobenzene. Yield 1.28 g (13%) m.p. >360°C. 

When a column becomes saturated with metal and has exhausted its ability to attract and hold more, it is regenerated by flushing the column with a suitable acid, caustic or brine solution (eluant). this solution restores the resin beads to their original condition and removes the metal from the columns in dissolved form. The resulting solution (eluate) is much more concentrated than the influent waste stream and is ideal for further treatment by electrcwinning. 

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