Brine collection

Hi) Salt from sea water Another principal application of electrodialysis is the production of common salt from sea water. In the manufacture of salt from this source, generally sea water is first filtered and then warmed with waste heat. Next, this water is slowly passed through the depletion compartments of the multicompartment electrodialysis equipment. Concentration of solids reaches about 20% by weight in the brine collecting in the enrichment compartments. Further processing of this concentrated brine by evaporation yields the salt in solid crystalline state. 

The density of the water in Don Juan Pond is exceptionally high. Meyer et al. (1962) reported a value of 1.2514 g/mL, whereas Yamagata et al. (1967) obtained 1.351 and 1.380 g/mL. Jones (1969) later determined a value of 1.2744 g/mL at 20°C in one sample of brine collected by D.D. Koob during the summer of 1964/65. The shallow depth of the brine (about 10 cm), the lack of an ice cover, and steady wind all prevent the brine from becoming stratified (Harris et al. 1979). 

The Sr/ Sr ratio of the brine in Don Juan Pond measured by Jones (1969) was confirmed by Friedman et al. (1995) who reported values of 0.7185 for brine collected on January 10, 1975 0.7186 for crystals of antarcticites collected in November of 1973 and 0.7187 for interstitial brine from sediment at a depth of 10.8 m. They also reported that the average Sr/ Sr ratio of glacial meltwater that is discharged into Don Juan Pond is 0.7163 0.0009 and that the average strontium concentration of the meltwater is only 0.086 0.011 ppm. Evidently, the strontium in the meltwater that flows into Don Juan Pond is derived by chemical weathering of silicate minerals in the soil west of the pond and marine strontium is not detectable in the water of the tributary streams. The hterature containing information relevant to the study of Don Juan Pond is listed in Appendix 19.9.4. 

A. Depleted Brine Collection. A depleted brine receiver (or anolyte tank) collects overflowing brine from the electrolyzers (Rg. 11.13). Addition of HCl releases tbe chlorine dissolved in the brine. By way of the depleted brine header, this vessel also receives the flushing brine when the rectifiers trip. Space constraints may prevent the use of a tank with enough freeboard to accept all the flushing brine. This situation is addressed in Section 11.2.2.5E. 

E. Dechlorinated Brine Surge Tank. If the depleted brine receiver cannot hold the volume required to flush the ceUs during the rectifier shutdown, a surge tank of sufficient volume is necessary (Fig. 11.17). The brine collected in this tank can be returned to the brine system at a controlled rate. The same tank can receive brine diverted from the process for other reasons. The diversion system shown here consists of a pair of on-off valves, one in the brine line after the neutralization system and the other in the line to the dechlorinated brine hold tank. Dechlorinated brine ean be diverted into this tank manually or automatically. Reasons for automatic diversion include power failure and insufficient dechlorination. 

Figure XXIV-23 shows the routing of input, output and internal mass fluxes. Fresh seawater enters the site from the open ocean into the man-made harbour and then moves down the canals separating the peninsulas. These canals feed the desalination plants brine exits to the right into a brine collection canal running between the BOPs and reactors. This brine discharge canal circles around the reactors. This circuitous route is taken to avoid the need for multiple bridges under the heavy capacity railroad in Fig. XXIV-23. The brine is rejected from the desalination plant at 10°C above the seawater inlet temperature - a normal practice for desalination plants - and the extended travel time of the brine from BOP back to the ocean allows opportunity for further cooldown of the brine before return to the sea. Alternately, that heat and brine may be put to profitable use such as heating acres of greenhouses or perhaps shellfish beds.

A solution of 2,3-dibromo-5-methoxyaniline (32 g, 0.17 mol) in CHjClj (300 ml) was stirred and cooled in an icc bath. Boron trichloride (1 M in CH2CI2, 180 ml, 0.18 mol), chloroacetonitrile (14.3 g, 0.19 mol) and TiC (1 M in CH CIj, 190ml, 0.19 mol) were added. The resulting mixture was refluxed for 1.5 h. The solution was cooled to room temperature and poured carefully on to a mixture of icc and 20% aq. HCl (700 ml). The organic layer was separated and the CH Clj removed by distillation. The residue was heated to 90°C on a water bath for 30 min. The solution was cooled and the solid collected by filtration. It was partitioned between ether (1.41) and 1 N NaOH (500 ml). The ether layer was washed with brine, dried over Na2S04 and evaporated. The residue was recrystallized from ethanol to give 2-amino-3,4-dibromo-6-methoxy-a-chloroacetophenone (55 g) in 90% yield. 

Current is fed into the electrolyzer by means of anodic and cathodic end elements. The anodic compartment of each cell is joined to an independent brine feed tank by means of flanged connections. Chlorine gas leaves each cell from the top, passing through the brine feed tank and then to the cell room collection system. Hydrogen leaves from the top of the cathodic compartment of each cell the cell Hquor leaves the cathodic compartment from the bottom through an adjustable level connection. 

Other Processes. Dead Sea Periclase (DSP, Mishor Rotem, Israel) converts magnesium chloride into MgO by spray-roasting, then hydrates the MgO to Mg(OH)2. The Mg(OH)2 is washed and dmm filtered. DSP purchases the brine from Dead Sea Works, which collects and stores enriched brine from the southern margins of the Dead Sea (77). 

Electrodialysis Reversal. Electro dialysis reversal processes operate on the same principles as ED however, EDR operation reverses system polarity (typically three to four times per hour). This reversal stops the buildup of concentrated solutions on the membrane and thereby reduces the accumulation of inorganic and organic deposition on the membrane surface. EDR systems are similar to ED systems, designed with adequate chamber area to collect both product water and brine. EDR produces water of the same purity as ED. 

The sodium chlorate manufacturing process can be divided into six steps (/) brine treatment 2 electrolysis (J) crystallisation and salt recovery (4) chromium removal (5) hydrogen purification and collection and (6) electrical distribution. These steps are outlined in Figure 3. 

Methyi-2,2-dlphenyicyclopropane (2). A mature of NaNH2 (3.0 g. 75 mmol) and 1-benzoyl-1 methyl-2,2-diphenylcyciopropane 1 (9 3 g, 30 mmol) in PhMe (80 mL) was refluxed lor S h. The cooled reaction mixture was treated with cracked ice (50 g) and the separated organic layer, after washing with brine was distilled. The fraction bp 106-1 OT C (2.5 mm) was collected. There were obtained 4 9 g ol 2 (79%). 

Modem cells employ arrays of anodes (Ti02 coated with a noble metal) and cathodes (mild steel) spaced 3 mm apart and carrying current at 2700Am into brine (80-100gl ) at 60-80°C. Under these conditions current efficiency can reach 93% and 1 tonne of NaC103 can be obtained from 565 kg NaCl and 4535 kWh of electricity. The off-gas H2 is also collected. 

Where a secondary refrigerant fluid is to be circulated, and the working temperatures are at or below 0°C, then some form of nonfreeze mixture must be used. These are collectively termed brines. 

A mixture of 7-chloro-5-phcnyl-17/-l,4-benzodiazepin-2(3//)-one (271 g, 1.0 mol), P2S3 (242 g, 1.09 mol) and pyridine (2 L) was refluxed with stirring for 45 min. The resulting solution was cooled in an ice bath and poured slowly into ice-cold sat. brine (5 I.). The precipitated solid was collected, washed with H20, dried and dissolved in CH2C12. The solution was filtered through a bed of activated alumina and con-... 

In highly saline brines, which were collected from the Vassar Vertz Sand Unit, Pajme County, Oklahoma, diverse populations of anaerobic, heterotrophic bacteria were present. All strains grew in a mineral salts medium containing glucose, yeast extract, and casamino acids in the presence of NaCl concentrations of up to 20% by weight [177],... 

To conclude this section, reference may be drawn to what is called the Placid process for recycling lead from batteries. Placid denotes the leaching of lead in warm, slightly acidic, hydrochloric acid brine to form soluble lead chloride. Lead is won from the lead chloride on the cathode of an electro winning cell and is collected. Chloride anions are released simultaneously, but then react immediately with hydrogen ions that have been produced stoichio-metrically from electrolysis of water in the anolyte and passed into the catholyte through a membrane. The hydrochloric acid that is formed is returned as a make-up content to the leaching bath. 

This type of electrolytic cell consists of anodes and cathodes that are separated by a water impermeable ion-conducting membrane. Brine is fed through the anode where chlorine gas is generated and sodium hydroxide solution collects at the cathode. Chloride ions are prevented from migrating from the anode compartment to the cathode compartment by the membrane and this, consequently, leads to the production of sodium hydroxide, free of contaminants like salts. The condition of the membrane during operation requires more care. They must remain stable while being exposed to chlorine and strong caustic solution on either side they must allow, also, the transport of sodium ions and not chloride ions. 

The core - flood apparatus is illustrated in Figure 1. The system consists of two positive displacement pumps with their respective metering controls which are connected through 1/8 inch stainless steel tubing to a cross joint and subsequently to the inlet end of a coreholder 35 cm. long and 4 cm. in diameter. Online filters of 7 im size were used to filter the polymer and brine solutions. A bypass line was used to inject a slug of surfactant solution. Two Validyne pressure transducers with appropriate capacity diaphragms are connected to the system. One of these measured differential pressure between the two pressure taps located about one centimeter from either end of the coreholder, and the other recorded the total pressure drop across the core and was directly connected to the inlet line. A two - channel linear strip chart recorder provided a continuous trace of the pressures. An automatic fraction collector was used to collect the effluent fluids. 

A micellar flood was then started with the injection of the micellar slug, polymer buffer, and the drive water in succession, at a rate of 1.3 m/day. Two types of polymers - polyacrylamide polymer (Dow Pusher 700) and Xanthan Gum polymer (Kelzan XC) - were used as the polymer buffers. Sodium chloride brine (1%) was used as the drive water. Effluent was collected and analyzed for surfactant content using the IR and UV techniques. 

---