Showing papers on "Brine published in 1973"

A Low-Tension Waterflooding Process

Abstract: Laboratory and field work using polymer and surfactant slugs for tertiary recovery in watered-out fields led to the conclusion that an oil bank can be formed in a sandstone reservoir using low-tension surfactants. It is essential that the mobility behind the bank be controlled to insure maximum recovery of mobilized oil. The surfactant used in the field tests was a commercial petroleum sulfonate blend with an equivalent weight of about 415. In order to protect the surfactant, an aqueous solution of sodium chloride was injected prior to the surfactant to screen the low-tension sulfonate from the reservoir brine and to base exchange the reservoir solids, replacing magnesium and calcium with sodium ions. Sodium tripolyphosphate or sodium carbonate, or both, is added to the rear portion of the surfactant slug to reduce adsorption and to improve water-wetness of the reservoir rock surfaces. The mobility control slug injected after the surfactant consisted of a water-soluble biopolymer in combination with sodium chloride of concentration less than the minimum that provides very low tension. Field testing was done on a producing sand in the Loma Novia field, Duval County, Texas. Recoveries were not given in terms of barrels per day or percent, although themore » author stated that oil cuts peaked in two wells at 20 percent and 12 percent.« less

Transient and steady‐state salt transport between sediments and brine in closed lakes

Abstract: A diffusional transport model for Lake Abcrt, Oregon, predicts the rates of salt transport from pore fluids into lake waters. In a lake without outflow clissolved salts may migrate across the sediment-water interface in response to a concentration difference between lake and interstitial brine. Transport of salt upward is transient; its direction can be reversed by external input of salt or by dcplction of salts stored in the sediments, and a steady-state concentration in lakc water is not attainable. Downward transport can be a stationary process if the sedimentation rate is rapid compared with molecular diffusion of salt in interstitial brine, but characteristic rates arc too slow to lead to steady-state concentrations within the lifetime of a closed lake. In Lake Rbert, diffusional flux upward was much more important than input of salt from other sources; 45% of the salt of lake brine in 1963-1964 was added from the sediment port space during the preceding 25 years, only 0.1% from external inflow. The sediment source will dominate input during high water level. Sucl~ ~uodcls permit comparison of salt transport across the sediment-water interface with other input so~nccs at different times of the lake’s history.

Photooxidizing organic contaminants in aqueous brine solutions

Abstract: Disclosed herein is a novel, relatively fast method for reducing the concentration of water soluble carboxylic contaminants, (e.g., acetate ion, acetic acid, or salts thereof) in chloride containing brines. The method comprises contacting the brine stream with chlorine and ultraviolet light and controlling the pH of the brine.

Vacuum freezing vapor compression apparatus

Abstract: Method and apparatus are provided for recovering a solvent from a solution, particularly useful for recovering potable water from saline water. A unitary apparatus for minimum heat exchange with the environment is described, with the interior divided into a plurality of chambers. Saline water is flash evaporated in an evacuated chamber to produce water vapor, ice crystals, and a somewhat more concentrated brine. The brine-ice slurry is transferred to a washing column wherein it moves upwardly by hydraulic action to overflow the brine into a brine chamber. Ice floating in the wash or separation chamber is cleansed of brine by fresh water sprays. Ice at the top of the separation chamber is scraped by a continuous conveyor to the top of a melting chamber, into which it is free to drop through a grate. Water vapor from the freezing chamber is compressed and discharged into the bottom of the melting chamber with a sufficient flow to form a fluidized bed with the ice crystals entering the top of the chamber. Heat exchange between the water vapor and ice crystals causes condensation and melting, respectively, to produce potable water. Refrigeration coils may be provided for condensing excess water vapor in a flow path beyond the fluidized bed.

Ion exchange removal of dichromates from electrolytically produced alkali metal chlorate-chloride solutions

Abstract: IN AN ELECTROLYTIC PROCESS IN WHICH ALKALI METAL CHLORATE IS PRODUCED FROM ALKALI METAL CHLORIDE SOLUTION, DICHROMATES (UTILIZED FOR CATHODIC PROTECTION DURING ELECTROLYSIS) ARE REMOVED FROM AN EFFLUENT STREAM OF CHLORATE ENRICHED SOLUTION BY PASSING THE STREAM THROUGH AN ION EXCHANGE RESIN TO EFFECT AN IMPROVEMENT IN PROCESS EFFICIENCY. WHEN THE ION EXCHANGE RESIN BECOMES EXHAUSTED THE BED IS REGENERATED WITH HIGH PH SODIUM CHLORIDE BRINE. THE ION EXCHANGE SYSTEM IS ESPECIALLY ADAPTED TO REMOVE DICHROMATES FROM THE RECYCLE STREAM OF THE EVAPORATIVELY CONCENTRATED ALKALI METAL CHLORATE SOLUTION WHEREBY THE RECYCLE STREAM CAN BE COMBINED WITH THE ELECTROLYTIC PROCESS EFFLUENT FOR EVAPORATIVE CONCENTRATION.

Method of producing sodium carbonate and bicarbonate spherules from brine

Abstract: Free-flowing spherules of sodium bicarbonate are prepared from a sodium carbonate or from salt brine, substantially saturated with ammonia, by carbonating the sodium carbonate solution, or the ammonia-saturated brine with carbon dioxide in the presence of from 200 to 2500 parts per million of a water soluble alkaline phosphate. Spherules of sodium bicarbonate crystallizing from the solutions are separated as a product having a bulk density between about 32 to 48 pounds per cubic foot, and a screen size substantially between 14 and 100 mesh. Sodium carbonate spherules are also readily obtained by calcining the sodium bicarbonate spherules.

Electrolytic method for the manufacture of chlorates

Abstract: Chlorates, such as alkali metal chlorates, are made by electrolyzing brine in a cell having a plurality of compartments or zones therein preferably three, wherein anode and cathode compartments are separated by a buffer compartment formed by permselective membranes of a hydrolyzed copolymer of tetrafluoroethylene and a fluorosulfonated perfluorovinyl ether, or a sulfostyrenated perfluorinated ethylene propylene polymer, or by such a permselective membrane on the cathode side plus a porous diaphragm on the anode side, while reacting chlorine gas with the buffer zone contents in the zone or removed from it, while being under such conditions as to produce hypochlorite and/or chlorate and chloride therein, converting any hypochlorite to chlorate and chloride, and passing a solution of such chlorate and chloride in a liquid medium into the anode compartment and electrolyzing the chloride thereof. By such a process, with continued recirculation of the product solution until the chlorate content is sufficiently high, a relatively concentrated chlorate solution can be produced containing proportionally less chloride, due to its conversion to chlorate, and obviating the need for additional processing to remove chloride before chlorate could be obtained low in chloride and at an acceptable concentration.

Control for absorption refrigeration system

Abstract: Controls for an absorption refrigeration machine which is constructed to operate in a normal manner wherein an absorbent solution is utilized as the driving force to absorb vapor released under subatmospheric conditions from a refrigerant, such as water, and also in a mode wherein the cooling water circulated through the absorber tube bundle condenses refrigerant vapor released from the evaporator tube bundle. A pan is located between the normal solution level in the absorber and the absorber heat exchanger which empties into the absorber sump during normal operation but functions as a receiver for refrigerant during the ''''free cooling'''' operation. This construction eliminates the requirement for an auxiliary receiver to hold the solution or brine during free cooling operations.

Method for removing sulfate and bicarbonate ions from sea water or brackish water through the use of weak anionic exchange resins containing amino groups of the primary and secondary type

Abstract: R-CL+SO2=->R-SO4+CL- SAID BICARBONATE IONS IN SAID SEA WATER OR BRACKISH WATER BEING ELIMINATED BY THE HYDROLYSIS OF SAID RESIN ACCORDING TO THE FOLLOWING EQUATIONS: R-CL+H2O->- CO2+H2O 1. A METHOD FOR REMOVING SULFATE AND BICARBONATE IONS FROM SEA WATER OR BRACKISH WATER PRIOR TO BEING SUBJECTED TO DESALINATION IN A CONVENTIONAL DESALINATION PLANT, WHICH COMPRISES: PERMITTING SAID SEA WATER OR BRACKISH WATER TO PASS THROUGH A BED CONTAINING THE CHLORIDE FORM OF A WEAK ANIONIC RESIN HAVING AMINO FUNCTIONAL GROUPS OF THE PRIMARY AND SECONDARY TYPE, SAID CHLORIDE FORM OF SAID RESIN BEING EXPRESSED AS R-CI, THUS PERMITTING THE SULFATE IONS IN SAID SEA WATER OR BRACKISH WATER TO BE EXCHANGED FOR THE CHLORIDE IONS OF SAID RESIN BY THE FOLLOWING EQUATION: AND SUBSEQUENTLY, REGENERATING SAID RESIN TO THE CHLORIDE FORM, WHEN SAID RESIN IS EXHAUSTED, BY PERMITTING THE BRINE SOLUTION DISCHARGE FROM THE DESALINATION PROCEDURE AND HAVING A SALT CONCENTRATION OF AT LEAST 1.5 TIMES GREATER THAN THAT OF SAID SEA WATER OR BRACKISH WATER TO CIRCULATE THROUGH SAID BED CONTAINING SAID RESIN HAVING SAID AMINO FUNCTIONAL GROUPS OF THE PRIMARY AND SECONDARY TYPE, THE CHLORIDE/SULFATE RATIO OF SAID BRINE SOLUTION BEING AT LEAST 3 TIMES GREATER THAN THAT OF SAID SEA WATER OR BRACKISH WATER TREATED, AND THE PH OF SAID BRINE SOLUTION BEING BETWEEN 4 AND 5 TO DISPLACE REACTION (2) ABOVE, TO THE LEFT.

PROCESS FOR THE PREPARATION OF ANHYDROUS MgCl PRILLS

Abstract: The process prepares magnesium chloride prills suitable for the electrolytic production of magnesium from a melt. Molten magnesium chloride hydrate having a moisture content corresponding to from about 3.8 to about 6.2 moles of H2 O per mole of MgCl2 is converted into droplets which are solidified to form prills. The prills are dehydrated to the desired low-moisture magnesium chloride or substantially anhydrous magnesium chloride. The invention relates to a process for preparing magnesium chloride suitable for the electrolytic production of magnesium metal, and more particularly it relates to a process for the preparation of magnesium chloride in the form of firm prills suitable to be charged as such to the electrolytic cell. The term "prill" is here intended to mean small bodies above about 0.15 mm in size, thus excluding the very small particles that are produced by the spray-drying technique. Magnesium metal is preponderantly produced by molten salt electrolysis of magnesium chloride. According to a well known electrolytic process, the magnesium chloride is anhydrous chloride, while another well known electrolytic process employs hydrated chloride corresponding to about 2 moles of H2 O per mole of MgCl2. When preparing anhydrous and low-moisture magnesium chloride for electrolysis, it is of great interest, as is well known, to utilize magnesium chloride brines obtained in the industrial treatment of various natural salt deposits and saline waters. Commercial magnesium chloride brines usually are saturated aqueous solutions of magnesium chloride, corresponding to 10-12 moles of H2 O per mole of MgCl2. In the preparation of magnesium chloride for electrolysis it is known to spray-dry the aqueous chloride solution in a high tower in counter-current with for instance air, whereby fine magnesium chloride powder can be obtained containing for instance 0.5-1 mole of H2 O per mole of MgCl2. While this method provides a high degree of dehydration it entails a very great loss in the form of a fine dust which is carried away by the drying gas used and which in a great part cannot be recovered economically. The particle size is mostly below 15 microns. The loss in the form of dust would be about 20 percent. The product obtained can be accumulated by melting. Another known process comprises spray drying a concentrated magnesium chloride solution to a moisture content corresponding to the dihydrate or a little lower and effecting the further dehydration in a fluidized bed in the presence of HC1 gas. In this process the particle size is 20-100 microns, and with such particle sizes the fluidized bed treatment must be carried out at very low gas velocities. As a consequence thereof the dimension of the fluidized bed apparatus will have to be quite large. To avoid this it has been proposed to treat the spray dried powder between rolls to form flakes, which are then broken up to the extent desired, whereafter the product thus obtained is subjected to fluidized bed drying with HC1 gas. The process is thereby made considerably more complex. Further it is known to reduce the moisture content of magnesium chloride brine by spraying a molten magnesium chloride hydrate into a fluidized bed of partly dehydrated magnesium chloride particles, which for instance can be recirculated solid particles, or they can be crystals of for instance the hexahydrate of magnesium chloride which is readily available. In this process the dehydration in principle is presumed to occur as the molten phase hits the solid phase particles so that evaporation takes place from the surface thereof. Also in these latter processes for the dehydration of magnesium chloride the loss in the form of dust is considerable. By means of the present invention the abovementioned drawbacks are avoided. The process of the invention has enabled magnesium chloride hydrate to be directly made into prills of a very suitable size and having a quite satisfactory mechanical strength, both for the further dehydration to anhydrous or to low-moisture magnesium chloride as well as for the final utilization of the prills as feed material to the electrolytic cells. Surprisingly it has turned out that prills of the above-mentioned type can be obtained when molten magnesium chloride hydrate having a moisture content corresponding to from about 3.8 to about 6.2 moles of H2 O per mole MgCl2 is made into granules or prills by prilling the melt from a centrifuge or through a perforated plate or other suitable prilling means to form droplets which are converted into (prills solidified spheroidal grains), by cooling in a gaseous or liquid cooling medium, whereafter the prills obtained are dried to give the desired low-moisture magnesium chloride, or the anhydrous magnesium chloride as the case may be. The first step in the process of the invention thus in short, is to subject magnesium chloride melt of the above-mentioned degree of hydration to a prilling process, and the invention is based on the finding which we have ascertained by extensive research and experiments, that one can thereby provide granules which are excellently suitable for being progressively dehydrated as well as for the eventual use as electrolytic cell feed material for the production of magnesium. Other aspects of the invention will be apparent from the following detailed description including examples showing how to carry out the process of the invention in practice.

Production of high purity salt from high sulfate salt deposits

Abstract: A subterranean salt deposit is solution mined, and the resulting calcium- and sulfate-contaminated brine is treated, e.g., by soda ash, to precipitate insoluble calcium compounds. The resulting slurry is settled, and the effluent clear brine is evaporated in a series of solar ponds to produce high-grade sodium chloride. The brine becomes progressively more concentrated with respect to sodium sulfate as it moves through the solar ponds. The sulfate-enriched brine may be recycled to the solution mine, evaporated to form a sulfate-contaminated sodium chloride crystal crop, or it may be subjected to winter cooling to remove sulfate values as Glauber's salt, the residual brine being recycled to the solar ponds or the solution mine.

Displacement of a micellar slug foam in unconsolidated porous media. [Comparison of micellar slug driven by foam versus by a polymer flood]

Abstract: A comparison of a micellar slug driven by a foam versus by a polymer flood was made. The aqueous slug contained Floodaid 130 and brine (2 percent sodium chloride). Foam was generated from an aqueous brine solution of Triton X-100. The polymer flood was Dow Chemical's P-700 in the brine. Sand packs (porosity 39.4 percent, permeability 23.6 d) were saturated with the brine and flooded with 32.5/sup 0/ API California waxy crude oil. For secondary oil recovery, the slug-foam treatment obtained about 25 percent less of the original oil in place than the slug-polymer treatment. However after waterflooding with the brine, tertiary recovery by the slug-foam treatment was only about 8 percent less than the amount obtained by the slug followed by a polymer flood. Hence, tertiary oil recovery using a foam drive fluid could be economically attractive since less foaming agent than polymer is required.

Method for recovering fresh water from brine

Abstract: A process is disclosed for recovering fresh water from brine which includes introducing brine, which has been inoculated with a predetermined number of ice nuclei and is at about its freezing temperature, into an elongated crystal growth zone which is supplied with refrigerant along the brine flow path at a graduated rate such that more refrigerant is supplied toward the outlet of the crystal growth zone than near the inlet. Ice crystals are separated from the resulting brine-ice slurry, and the ice crystals are washed with fresh water before being melted to recover fresh water.

Process for pretreating sea water by preheating same in the preparation of brine and fresh water

Abstract: A process for pre-treating sea water in the preparation of brine and fresh water from the sea water by heating in a multiple effect, multi-stage flash evaporator comprising taking the sea water to be treated out of the end of a heat recovery tube, which is at a temperature of 40 DEG to 55 DEG C, in the flash evaporating apparatus, elevating the temperature of the sea water up to approximately 50 DEG to 65 DEG C by heat exchanging it with the drain from the heat-exchanger for heating in the flash evaporating apparatus, removing calcium from the sea water in a calcium separating tank at a calcium removal rate of 80 to 99%, adjusting the pH of the sea water to pH 5.0 to 5.5 and deaerating it. The deaerated sea water is returned to the latter part of the first effect tank in the evaporating apparatus so that the temperature of the said pre-treated sea water becomes as close as possible to that of the sea water which is initially taken out of the heat-exchanger in the flash evaporating apparatus to minimize the possible energy loss of the flash evaporating apparatus.

Bis(6-methyl-2-pyridyl)glyoxal dihydrazone as a spectrophotometric reagent for the rapid determination of copper in alkalis, milk and brine

Abstract: The synthesis, characteristics and analytical applications of bis(6-methyl-2-pyridyl)glyoxal dihydrazone are described. This compound produces coloured solutions selectively with copper(I) ions (λmax.= 440 nm, Iµ= 8·7 × 103 l mol–1 cm–1) that can be extracted into various organic solvents; it behaves as a cuproine-type reagent. The 1:1 orange-yellow copper(I) complex has been used for the spectrophotometric determination of trace amounts of copper in saturated brine, alkalis and milk. The most important advantage of using this reagent is the total recovery of copper that is possible from ammoniacal solutions.

Ice crystal wash

Abstract: A slurry of ice crystals and brine or aqueous beverage solution is forced through a conduit against a counterflow of butane or Freon as a wash fluid. The wash fluid emerges from the conduit through perforated or porous wall portions to enter a brine tank in which brine separates from the wash fluid and is removed. Washed crystals emerge from the conduit in a melt tank containing wash fluid. The crystals are melted, separated from the wash fluid, and withdrawn as fresh water. The wash fluid is pumped from the brine tank to the melt tank to cause its counterflow through the ice crystals. Alternately, the wash fluid may be introduced along the length of the conduit to flow to both tanks and be recirculated.

Purification of sodium silicofluoride by slurrying with NaCl containing brine

Abstract: A process for the purification of sodium silicofluoride which comprises repulping sodium silicofluoride containing gypsum and/or phosphates as impurities in an aqueous solution containing sodium chloride for a time sufficient to effect a substantial removal of the impurities and thereafter recovering the purified sodium silicofluoride.

Freeze concentrating solns, esp fresh water from sea water - with vibration means to prevent ice build up

Abstract: A method of concentrating solns, esp washings, from the cellulose and chemical inds, or concentrates from foodstuffs ind, or for freezing out fresh water from salt water comprises vibrating mechanically or electromagnetically the heat exchange surface between the refrigerated medium and the brine to prevent the build up of ice and to break up the laminar boundary layer by the resulting turbulence

Process of avoiding mercury emission from mercury-using plants

Abstract: Eliminating emission of mercury in an alkaline chloride electrolysis plant, for example, is achieved by converting pre-purified waste water to flushing water through vacuum distillation. Hot brine from the electrolysis plant serves as a heat carrier for the vacuum distillation step.

Carbonation of ammoniacal sodium chloride brine

Abstract: Carbonation of ammoniacal sodium chloride brine in the ammonia soda process wherein a phenol-free or phenol deficient ammonia is used as make-up ammonia, the improvement being that one or more phenolic compounds are added to the process in an amount sufficient to reduce the carbon dioxide content of waste gas leaving the carbonation stage to less than 12 percent carbon dioxide.

Desalination plant - using freezing and centrifugal separation of sweet water ice crystals

Abstract: Seawater desalination plant which operates by freezing and separation of ice crystals whereby during freezing, a suspension of ice crystals is formed in a mother liquor and the suspension is centrifuged to give crystals of sweet water. The crystals form on the walls (6) of the vessel and are scraped off prior to centrifuging into the remelting chamber (9). Higher yield than existing methods. The brine which drains into collection tank (10) through perforations in the spinner (8); the cold brine is passed through heat exchanger (11) for pre-cooling the sea-water from the feed pump (1).

Brine valve assembly

Abstract: An improved brine valve assembly for control of the brine used to regenerate ion exchange material. The brine valve assembly includes a float valve arrangement for closing and sealing the inlet port when a predetermined low level is reached in the brine tank. The float valve is positioned to float within a float cage immediately prior to its sealing of the inlet port. The level of liquid within the cage is controlled through a tube having a lower end in communication therewith and an upper end in communication with the interior of the brine tank. The elevation of the upper end is adjustable to control the amount of brine drawn during each regeneration cycle. An alternative embodiment of the invention discloses a unique float construction which uses the weight of the brine to insure a better air shut-off.

Production of chloride-free potassium phosphates

Abstract: A PROCESS FOR THE PRODUCTING OF CHLORIDE-FREE POTASSIUM PHOSPHATE FERTILIZERS, CHLORINE AND HYDROGEN, INCLUDING A METHOD OF TREATMENT OF IMPURE SATURATED POTASSIUM CHLORIDE SOLUTION WHEREIN A PURE OR IMPURE BRINE IS ELECTROLYZED AT HIGH CURRENT EFFICIENCY. CHLORINE IS FORMED AT THE ANODE AND POTASSIUM AMALGAM, AT THE CATHODE. SAID AMALGAM IS SUBSEQUENTLY REACTED WITH ORTHOPHOSPHORIC ACID OR POLYPHOSPHORIC ACID SOLUTION AND WATER TO PRODUCE HYDROGEN AND POTASSIUM ORTHOPHOSPHATE OR POTASSIUM POLYPHOSPHATE SOLUTION, SOLIDS, AND SOLUTION WITH SOLIDS; OR AMALGAMS OF OTHER METALS, SUCH AS SODIUM, LITHIUM, AND ZINC ARE PRODUCED AT HIGH CURRENT EFFICIENCY FROM THEIR RESPECTIVE SIMILARLY TREATED IMPURE CHLORIDE BRINE FOR SUBSEQUENT PROCESSING.

Processes for decreasing mercury butter formation in mercury electrolytic cells

Abstract: Processes for decreasing mercury butter formation in mercury electrolytic cells employing brine which contains strontium wherein the brine is treated to lower the strontium content to 0.5 ppm or less. The removal of strontium from the brine may be effected by treating the brine with an ion exchange resin in sodium form to adsorb strontium thereon. Alternatively, strontium may be removed by treating the brine with a water-soluble metal hydroxide, subjecting the resulting mixture to partial evaporation to produce sodium chloride as precipitate and saturated brine solution and admixing the precipitate with water to form brine for electrolysis.