Showing papers on "Brine published in 1999"

Linkages between salinity and brine channel distribution in young sea ice

Abstract: A high-resolution study of bulk salinity was undertaken on laboratory-grown sea ice to determine the extent of spatial variability of salinity and whether this was associated with brine channel structures. Ice samples at two different stages of development were compared with respect to physical state, brine distribution, and brine channel structures. Cold, growing sea ice is shown to have steep bulk salinity gradients and a highly variable brine distribution that is closely linked to the location and morphology of brine channels. Areas of high bulk salinity are found to correspond directly to the positions of the brine channels, and these areas are surrounded by ice that shows significant brine depletion. It is observed that redistribution of the brine occurs as the ice cover goes through warming and melting phases. The redistribution is attributed to an increase in porosity and pore connectivity permitting migration of brine through the ice. The distribution of brine in “warm” ice is shown to be more homogeneous and independent of brine channel structures. A number of mechanisms exploiting the enhanced mobility of brine in warm sea ice are used to explain the changes in the salinity profiles and brine distribution.

Method for applying halide brines to surfaces

Abstract: A method for applying halide brine to surfaces requiring protection against freeze conditions, inhibition of snow and ice accumulating, deicing or freeze retardation, for example, or dust control with limited corrosion is disclosed, the method comprising the steps of forming an admixture of polyhydroxy carboxylate and polyalkoxylated amine dispersed in a halide brine solution in an amount effective to inhibit corrosion; and applying the admixture to surfaces. The method of this invention can be used to limit corrosion in the application of a halide brine to surfaces of dust-producing materials as well as surfaces requiring protection against freeze conditions.

Hydrographic changes during 20 years in the brine-filled basins of the Red Sea

Abstract: Many of the deep basins filled by hot brines in the Red Sea have not been investigated since their discovery in the early 1970s Twenty years later, in September 1992, six of these deeps were revisited The temperature and salinity of the Suakin, Port Sudan, Chain B, and Nereus deeps ranged from 2325 to 4460°C and from 144 to 270‰ These values were approximately the same in 1972, indicating that the budget of heat and salt was quite balanced We measured strong gradients of properties in the transition zone between brines and overlying seawater The contribution of salinity to the density gradient was more than one order of magnitude higher than the opposite contribution of temperature across the seawater–brine interface Therefore the interface was extemely stable, and the transfer of properties across it was considered to be controlled mostly by molecular diffusion We calculate that the diffusional transport of salt from the brines to seawater cannot affect significantly the salinity of the brines over a 20 year period, which agrees with the observations The brine pools can persist for centuries with no salt input Therefore, the persisence of brines does not correspond to a steady balance between diffusional loss and continuous input of hydrothermal solutions Deeps that experience only episodical hydrothermal brine supplies may persist for a long time with salt inherited from past inputs The theoretical loss of heat by diffusion from the brine to seawater was higher than the observed decrease in temperature of the brine pool during the 20 year period of observation We calculated that the heat flux out of the pools into the overlying seawater was compensated by a heat flux into the pools of about 250–600 mW/m2 This range of values corresponds to bottom heat flow values that have been reported earlier for the axial zone of the Red Sea In contrast to the other brine pools, the temperature and salinity of the Valdivia Deep brine increased by 41°C and 10‰, respectively, between 1972 and 1992, which is explained by present-day hydrothermal brine discharge

Surfactant-oil-water systems near the affinity inversion. Part XI. pH sensitive emulsions containing carboxylic acids

Abstract: Surfactant-oil-water systems in which the surface active substance is a mixture of carboxylic acid and its sodium salt (soap), exhibit emulsion property maps that are consistent with the phase behavior and the general emulsion phenomenology. However they present specific features such as an extended C+ multiple emulsion region and a skinked A+ W/O emulsion zone. In this case the aqueous phase pH drives the relative hydrophilicity of the acid/salt mixture at interface and plays the role of the most sensitive formulation variable. Studied systems contain C10 to C14 carboxylic acid, NaCl brine and a light distillation cut, as well as alcohols.

Drilling fluid systems with improved fluid loss properties

Abstract: A drilling fluid system comprising a brine and a quantity of cationic copolymers comprising a ratio of acrylamide monomers to cationic derivatives of acrylamide monomers, wherein the quantity and the ratio are effective to maintain effective rheology and fluid loss control in said drilling fluid system at temperatures of at least about 250° C. for at least about 16 hours.

Spent brine reclamation

Abstract: A method of reclaiming spent aqueous brine solutions used in the regeneration of water-softening resins is disclosed An aqueous chloride or other brine solution is acidified with HC1 to a pH of between about 05 and 6 and a soluble sulfate salt, preferably Na2SO4 is added, together with a precipitation inhibitor of the type polyacrylamide Following such treatment, the spent brine is pumped at high pressure axially through a spirally-wound nanofiltration-type membrane device which is effective to remove at least about 90 % of the divalent hardness while allowing passage therethrough of at least about 90 % of the monovalent cations As a result of such treatment, about 90 to 95 % of the volume of spent brine can be efficiently and effectively reclaimed in a form in which it is suitable for use again in regenerating water-softening resins or the like

Method for depositing snow-ice treatment material on pavement

Abstract: Apparatus and method for depositing salt granular materials upon a highway pavement at practical speeds. The deposition forms two narrow bands of the salt through utilization of two impeller-based mechanisms which are canted downwardly at an acute angle toward the pavement. The dump bed of trucks utilizing the apparatus is maintained in a down orientation through the utilization of a salt transport mechanism implemented as dual augers extending the length of the truck bed. Two embodiments of the apparatus are described each being self-contained and mountable upon a truck bed with relative ease. In one embodiment, a brine formation tank of generally triangular cross-sectional configuration is combined with a brine holding tank to form the sides of a V-box hopper structure. The brine formation tank is charged with salt and water to form a saturated brine which is permitted to migrate through a baffling system to the brine holding tank. A liquid pump system then drives the liquid to a cross auger apparatus wherein auger components are used as the mixing mechanism for adding brine to granular salt prior to its ejection to form the continuous narrow bands which are effective to attack the ice/pavement bond typically encountered on winter highways. The second embodiment utilizes the full capacity of the dump bed in conjunction with hydraulically biased contractor assemblies to move salt into a bed auger assembly.

Gel Systems for Controlling CO2 Mobility in Carbon Dioxide Miscible Flooding

Abstract: Conformance control for carbon dioxide miscible flooding using gel has not been widely attempted. Laboratory research efforts at the University of Kansas have produced promising in-situ gelation techniques aimed at this application. Three in-situ gel systems were developed and tested in laboratory cores. Two systems are based on a new biopolymer, termed KUSP1, and the third gel system uses the reaction of sulfomethylated resorcinol and formaldehyde to form a gel. KUSP1 gel systems were studied using two different methods of inducing in-situ gelation. In the first method, gelation was accomplished by injecting CO2 at low pressure into the Berea sandstone core saturated by alkaline polymer solution. Permeability reduction to the brine and CO2 in the range of 80% was achieved. Stability of the gel was tested in the presence of supercritical CO2 . When supercritical CO2 was used to induce in-situ gelation, the same degree of permeability reduction was achieved. The gel remained stable after the injection of many pore volumes of supercritical CO2 . The second method of initiating in-situ gelation involved the use of an ester. Hydrolysis of the ester, monoethylphthalate, in the alkaline polymer solution caused the pH to drop to levels where in-situ gelation occurred. The permeability of the treated core to supercritical carbon dioxide was about 1 md which was equivalent to a permeability reduction of 95%–97% of the initial brine permeability. The third gel system, based on the reaction of sulfomethylated resorcinol and formaldehyde ~SMRF!, was gelled in situ and contacted with both brine and supercritical CO2 . Permeabilities to carbon dioxide on the order of 1 md or less were observed. This permeability is equivalent to a reduction of about 99% in the initial brine permeability. Reduced permeabilities were maintained after injecting many pore volumes of supercritical CO2 and brine.

Field Tests on Silica Removal from Geothermal Brines in Sumikawa and Onuma Geothermal Areas

Abstract: In a study on prevention of silica scale formation in geothermal applications, two silica removal methods were examined using actual geothermal brine in the Sumikawa and Onuma geothermal areas: one was the addition of silica gel seeds. The other was the addition of aluminum ions. The results for silica gel seed show that the material precipitates on the seeds withdrawn from Sumikawa and model geothermal brine is only silica. On the other hand, the seeds withdrawn from Onuma brine contain not only silica but a small amount of aluminum. In the case of aluminum ion addition, the deposits withdrawn from Sumikawa geothermal brine contain not only silicon and aluminum, but also sodium, potassium and calcium. The composition of the deposits is similar to that of common silica scale. Also, the distribution ratios of these elements between the deposits and the brine are consistent with their common distribution ratios between silica scale and brine. In each case of silica gel seed and aluminum ion addition, the silica removal performance in the actual geothermal brines is found to agree with that in the model ones. Therefore results obtained in model geothermal brine can be applied to actual geothermal brine.

Process for obtaining monohydrated lithium sulfate from natural brines

Abstract: A process for obtaining monochlorated lithium sulfate from natural brines by mixing two brines: one saturated or nearly saturated with silvite (KCl), carnallite (KCl, MgCl 2 .6H 2 O), and lithium sulfate (Li 2 SO 4 .H 2 O), with a magnesium content of 4.7-6%, 0.8-1.2% lithium, and 1.2-4.2% total sulfate; and the other brine is saturated with bischofite (MgCl.6H 2 O), monohydrated lithium sulfate (Li 2 SO 4 .H 2 O), and carnallite (KCl, MgCl 2 .6H 2 O), and with a lithium content of 2.5-6%, below 6% magnesium, and less than 0.2% total sulfate, such that the resulting brine achieves a lithium sulfate content that exceeds its solubility in the brine, hereby it precipitates as monohydrated lithium sulfate. Crystallization can be accomplished in three stages in order to separate the carnallite from the lithium sulfate by filtering and washing it so as to enhance its purity and then drying the product if the goal is to retain anhydrous lithium sulfate.

Study of the Evaporation of a Brine Involving the System Na+, Mg2+, K+, Cl−, S 4 2− –H2O: Crystallisation of oceanic salts

Abstract: The evaporation of a Tunisian brine sample involving the system Na+, Mg2+, K+, Cl−, S 4 2− –H2O was studied under atmospheric pressure and at ambient temperature. The selective densities of precipitation of halite (NaCl) and of co-precipitation of halite and astrakanite (Na2Mg(SO4)2·4H2O), halite and kainite (MgSO4·KCl·H2O) and epsomite MgSO4·7H2O were determined.

Water softener salt formulation

Abstract: The monosodium and monopotassium citrates are improved iron-sequestering agents in salt compositions for regenerating spent water softener cation exchange resins. The dry compositions comprise a surfactant, an alkali metal chloride selected from the group consisting of sodium chloride and potassium chloride, and an iron sequestering agent selected from the group consisting of monosodium citrate and monopotassium citrate. The composition is preferably provided in the form of compacted pellets or blocks. The method for regenerating the spent cation exchange resin bed comprises the step of contacting the resin bed with an aqueous brine solution containing the citrate and a surfactant and having a pH of about 3.5 to 4.5.

Process and apparatus for purification of chlorine gas contaminated with bromine

Abstract: The flow of chlorine gas is washed in a column (5) with an aqueous solution comprising a low-salt brine extracted from downstream of electrolyzers (3) producing chlorine by electrolysis of brine. The brine washing is carried out in back flow, preferably with the chlorine gas flowing upwards, at a temperature of between 10 and 35 degrees C, and preferably between 15 and 20 degrees C. In addition, downstream of the washing process, the bromine and chlorine are separated from the brine by stripping using water vapor under vacuum or with a gas, preferably air. The process is operated on the site of chlorine production by electrolysis. The low-salt brine is cooled before washing the chlorine. The heat from the cooling process is used to carry out the stripping process. After stripping, the low-salt brine is recycled to upstream of the electrolysis units. At least one purge is put into this recycling line. An Independent claim is also included for the device for carrying out this process, comprising a unit producing chlorine by electrolysis of brine, a washing column for the gaseous chlorine, and a circuit carrying a fraction of the low-salt brine, taken from downstream of the electrolyzers (3) to the washing column (5). The device also contains a stripping unit (7) for removing chlorine and bromine from the brine after the washing process. A heat exchanger (E1) cools the brine before it enters the column and warms the brine leaving the column before it enters the stripper.

System for recovering glycol from glycol/brine streams

Abstract: A system for recovering glycol from glycol and brine mixtures produced from oil or natural gas wells that combines energy efficiency with a capability for handling salt and other solids contained in the mixture. The system comprises three effect evaporator systems in series. Each effect evaporator system comprises an evaporator, a separator vessel, product pumps, and a solids removal system. The process utilizes the system to remove salt and other solids as well as excess water leaving a glycol stream that can be reused as a hydrate inhibitor. The process begins by preheating a glycol/brine stream comprising approximately fifty percent (50%) glycol. The stream is then subjected to three evaporation cycles. The first evaporation cycle comprises introducing the preheated stream into a suppressed boiling point evaporator where the stream is heated under a constant pressure. The stream pressure is then dropped to cause a portion of the water contained in the stream to vaporize or flash. The flashing stream is then introduced into a separator vessel where the water vapor is separated from the remaining liquid stream. The water vapor is removed from the separator and condensed. The remaining liquid glycol/brine stream is then pumped from the separator vessel through a solids removal system where precipitated salts and solids are removed. These steps are repeated two additional times. Each time the remaining liquid stream becomes more concentrated with glycol until the finished product is approximately ninety percent (90%) glycol.

Control method for ice storage air-conditioning system

Abstract: PROBLEM TO BE SOLVED: To save the energy at a low load by controlling the brine circulation flow rate according to the fluctuation of the load to increase/decrease the power consumption of a circulation pump. SOLUTION: This air-conditioning system comprises a brine passage to connect a circulation pump 1', a heat source unit, an ice storage tank 3, a heat exchanger 4, and a control valve, and a cold and hot water passage to connect the heat exchanger 4, an air-conditioning loads and a cold and hot water circulation pump 5, the brine is cooled by the heat source unit, the water in the ice storage tank 3 is frozen by the brine to store the heat, the brine is cooled by the melting heat of the ice in the ice storage tank 3 in the heat radiation mode, and led to the heat exchanger 4 to cool a cold water in the cold and hot water passage through the heat exchanger 4. An inverter is controlled to drive the circulation pump 1' and the heat source unit 2' constantly at the output below the rated value to control the flow rate of the circulation pump 1' and the capacity of the heat source unit 2'. COPYRIGHT: (C)2001,JPO

UO22+ and NpO2+ Complexation with Citrate in Brine Solutions

Abstract: Complexation of uranyl (UO2 2+) and neptunyl (NpO2 +) with citrate at high ionic strengths I(m) has been investigated by solvent extraction with HDEHP. β1 app values were obtained for I(m) between 0.3 m and 5.0 m NaCl. For NpO2 +, at pHm = 4.7–6.4 only the 1:0:1 complex was formed while for UO2 2+ at pHm 3.0 the 1:1:1 and 1:0:1 complexes were detected with the latter species more dominant. Values obtained for β1 app ranged from 2.62 ± 0.05 to 2.56 ± 0.03 for neptunyl and from 7.30 ± 0.04 to 7.03 ± 0.08 for uranyl as 1 increased from 0.3m to 5.0m NaCl. The β1 app values were used to estimate the concentration of citrate required in a neutral brine to provide a 10% competition with hydrolysis.

Decontamination method for contaminated soil

Abstract: PROBLEM TO BE SOLVED: To crack the contaminated groud region as widely as possible by freezing the region and sucking the intrasoil gas from the ground to extract the contaminated vapor. SOLUTION: A gas or liq. pressure injection line 2 using a compressor 1, etc., is prepared in the contaminated soil region 8 to be restored previously set according to information of the boring test, etc. A freezing pipe 5 for supplying a refrigerant and a pressure injection pipe 2 or further a suction pipe 6 connected to a suction pump 7 are built in a well bored in the region. An antifreeze (aq. calcium chloride soln.) called a brine is cooled to -20 to -30 deg.C and introduced into the freezing pipe 5 through a circulating pump to cool the ground. The frozen ground is then naturally thawed to ordinary temps. or heated and rapidly thawed, and the gas in the soil is sucked to extract the contaminated vapor.

A mixed formate and bromide brine used in drilling fluids

Abstract: The use of a saturated aqueous salt solution, comprising at least one formate salt and at least one bromide salt, in a drilling fluid. Said saturated aqueous salt solution comprises 40-50 % by weight of water and 50-60 % by weight of said salts in a weight ratio formate to bromide of 30:70 to 60:40. Preferred salts are alkali metal formates and bromides. The saturated aqueous salts solution has a density and a total salt content exceeding that of a saturated aqueous solution of said bromide salt.

Method for electrolyzing alkali metal chloride

Abstract: PROBLEM TO BE SOLVED: To provide an improved method for electrolyzing an alkali metal chloride which is made industrially more advantageous by solving the deterioration problem of an ion exchanger in a demirabiliting stage, as a method for electrolyzing an alkali metal chloride including a saturated brine perparing stage, an electrolyzing stage, a dechlorinating stage and the demirabiliting stage, with the demirabiliting stage formed by a separation tower packed with an ion exchanger and with dilute brine and water passed alternately through the separation tower. SOLUTION: A stage for adsorbing or decomposing and removing the residual chlorine in the dilute brine discharged from the dechlorinating stage is provided between the dechlorinating stage and demirabiliting stage, the dilute brine discharged from the demirabiliting stage is divided into two parts, 3-50% of the dilute brine is introduced into the stage for adsorbing or decomposing and removing the residual chlorine, and the remainder is circulated directly to the saturated brine preparing stage.

Sodium carbonate recrystallization

Abstract: The present invention provides a process for producing sodium carbonate monohydrate crystals by introduction of anhydrous sodium carbonate into a saturated sodium carbonate brine solution under conditions in which sodium carbonate monohydrate formation is favored. As the anhydrous sodium carbonate dissolves, the brine becomes supersaturated resulting in relief of supersaturation by formation of sodium carbonate monohydrate crystals. The process includes controlling supersaturation and its relief to achieve growth of existing sodium carbonate monohydrate crystals rather than nucleation and formation of new sodium carbonate monohydrate crystals. The resulting crystals are separated from insoluble impurities on a size separation basis.

Solar energy distillation apparatus

Abstract: A solar energy distillation apparatus (1) capable of easily converting raw water such as sea water to fresh water at a low cost by evaporating raw water by solar heat, and repeatedly and effectively utilizing condensation latent heat of the resulting vapor, comprising a basin portion (2) having a water panel (10) and a multiple-effect portion (3) having a plurality of distillation units (4) divided by partitions (5). The vapor (11) of brine of the water panel (10) generated by solar heat undergoes condensation on the surface of the partitions (5a) and turns to distilled water (12). In this instance, brine (6) contained in a cloth (7) on one of the surfaces of the partitions (5a) evaporates due to condensation latent heat and the resulting vapor (13) undergoes condensation on the surfaces of the partitions (5b) to be turned to distilled water (12). Thereafter, distilled water (12) and condensed brine (14) are recovered in the same way. This invention does not need any specific heating means at the initial evaporation portion which is a problem with the prior art, and can effectively turn brine to fresh water at a low cost by re-utilizing solar heat and condensation latent heat of the resulting vapor. When double-glass having colored inner glass is used for the solar heat incidence surface of the basin portion, condensation of the vapor on this surface can be restrained and greater amounts of the resulting vapor can be utilized at the multiple-effect portion.

Method for producing sodium chloride crystals

Abstract: The invention concerns a method for producing sodium chloride crystals starting with sodium chloride brine contaminated with potassium chloride and sulphate ions, which consists in: adding a calcium compound (32) to the brine (48) to crystallise the glauberite (35) which is eliminated; subjecting the resulting aqueous solution (40) which is collected and subjecting the mother liquor (41) of the sodium chloride crystallisation to a cooling process (42) to crystallise the glaserite (45).

Method of defrosting for brine cooling system

Abstract: PROBLEM TO BE SOLVED: To shorten defrosting operation time without relying on a defrosting heater by supplying a part of a high-temperature refrigerant and brine discharged from a compressor to a refrigerator as hot brine. SOLUTION: In a brine circuit 20, a brine cooled by a refrigerant is primarily stored in a low-temperature tank 21, flows out therefrom into a brine supply channel 25 and cools a refrigerator 41 for a show-case 40 by way of a show-case circulation pump 22 to cool the inside of the show-case 40 at a predetermined temperature. Brine raised in temperature by heat exchange in the refrigerator 41 is recovered to an intermediate-temperature tank 23 through a brine recovering circuit 26, and returned to a brine refrigerating flow path 15b for a cooling heat exchanger 15 by a heat exchange circulation pump 24. In a hot brine circuit 30, brine stored in a hot tank 31 is heated by a high- temperature refrigerant flowing through a heating flow path 31a.