Showing papers on "Raffinate published in 2010"

Simulated moving bed chromatographic separation process for the purification of polyunsaturated fatty acids

Abstract: The present invention provides a chromatographic separation process for recovering a polyunsaturated fatty acid (PUFA) product, from a feed mixture, which process comprises introducing the feed mixture to a simulated or actual moving bed chromatography apparatus having a plurality of linked chromatography columns containing, as eluent, an aqueous alcohol, wherein the apparatus has a plurality of zones comprising at least a first zone and second zone, each zone having an extract stream and a raffinate stream from which liquid can be collected from said plurality of linked chromatography columns, and wherein (a) a raffinate stream containing the PUFA product together with more polar components is collected from a column in the first zone and introduced to a nonadjacent column in the second zone, and/or (b) an extract stream containing the PUFA product together with less polar components is collected from a column in the second zone and introduced to a nonadjacent column in the first zone, said PUFA product being separated from different components of the feed mixture in each zone.

Thermo-mechanical behaviour of the raffinate resulting from the aqueous extraction of sunflower whole plant in twin-screw extruder: manufacturing of biodegradable agromaterials by thermo-pressing

Abstract: Biorefinery of sunflower whole plant can be realized using a twin-screw extruder. Thermo-mechanical fractionation and aqueous extraction are conducted simultaneously. A filter section is outfitted along the barrel to collect continuously an extract and a raffinate (cake meal). Oil yield obtained is 53%. Proteins are partly extracted at the same time, just as pectins and hemicelluloses. Protein yield is 46%. Cake meal is relatively moist (66% for the moisture content). It is first dried to make easier its conservation. It is largely composed of lignocellulosic fibres (59% of the dry matter) from depithed stalk. Lipid content is 13% of the dry matter or 35% of the oil in whole plant. Protein content is 7% of the dry matter or 45% of the proteins in whole plant. DSC measurements indicate that denaturation of proteins is almost complete in the cake meal. DMTA spectrum of its milled powder reveals a significant peak at high temperature (between 175 and 200°C). As already observed with industrial sunflower cake meal, it can be associated with the glass transition of proteins. As a mixture of fibres and proteins, the cake meal can be considered as a natural composite. It is successfully processed into biodegradable and value-added agromaterials by thermo-pressing. As for DMTA analysis, the glass transition of proteins in the cake meal is also observed with PVT analysis at around 180°C. It makes easier the choice of the best thermo-pressing conditions to produce panels with higher mechanical properties in bending. These properties increase simultaneously with temperature, pressure and time chosen for molding operation. The highest flexural strength at break (11.5 MPa) and the highest elastic modulus (2.22 GPa) are obtained for the next molding conditions: 200°C and 320 kgf/cm2 during 60 s. Drop angle measurements show that the corresponding panel is also the most resistant to water. No significant transition is observed inside this panel above 0°C and until 200°C with DMTA analysis. Proteins ensure the agromaterial cohesion without any phase change in this temperature range, and fibres entanglement also acts like reinforcement. This panel could be used as inter-layer sheets for pallets or for the manufacturing of biodegradable containers (composters, crates for vegetable gardening) by assembly of panels.

l-Ribose from l-arabinose by epimerization and its purification by 3-zone simulated moving bed chromatography

Abstract: L-Ribose has recently received attention as the starting material for nucleoside drugs. As it is not found in nature, it is being produced by enzymatic or epimerization reaction. We investigated an epimerization reaction by molybdenium oxide and examined the effects of temperature, solvent, and molybdenum oxide amount on epimerization. L-Ribose has a yield of 22% under the conditions of 100 kg/m3 L-arabinose, 20% methanol, 5 kg/m3 MoO3, and 90 degrees C. In addition, simulated moving bed (SMB) that was equipped with three NH2-HPLC columns was used to separate L-arabinose and L-ribose resulting from L-arabinose epimerization. A 3-zone SMB process was developed to eliminate the high pressure problem in the conventional 4-zone SMB. Aspen simulation was performed to determine the operating variables such as switching time, raffinate, and extract flow rates. Experimental purities of extract and raffinate were compared with the theoretical ones and they are found to be fairly well correlated.

Modeling of the FCC Gasoline Desulfurization Process by Liquid Extraction with Sulfolane

Abstract: Extractive desulfurization of fluid catalytic cracking (FCC) gasoline with sulfolane was studied in a batch apparatus. The influence of three inlet parameters (temperature, inlet sulfur content, and solvent ratio) on the process response, that is, desulfurization efficiency, was investigated with the use of a Box-Behnken experimental design by response surface methodology. A mathematical model that can be used for predicting sulfur content in raffinate after extractive batch processing with sulfolane was statistically developed and proven with analysis of variance. Statistical analysis showed that the largest influence on desulfurization efficiency was solvent ratio, the second most significant influence was inlet sulfur content, followed by temperature, and last the interaction between solvent ratio and inlet sulfur content. The obtained second-order polynomial model shows that maximum desulfurization efficiency of 65.34% can be achieved at temperature of 50°C and higher values of inlet sulfur c...

Recovery of Trace Rare Earths from High-Level Fe3+ and Al3+ Waste of Oil Shale Ash (Fe−Al−OSA)

Abstract: An experimental investigation was undertaken to study the high-efficient and clean enrichment of trace rare earths from high-level Fe3+ and Al3+ waste of oil shale ash (Fe−Al−OSA). The optimum leaching temperature, ratio of solid to liquid, acidity, and reaction time for Fe−Al−OSA were 30 °C, 1:7, 50% (v/v), and 1 h by the Taguchi method, respectively, and the leaching rate of rare earths has been reached up to 96.24%. The optimal extraction conditions for removing Fe3+ from leaching liquor of Fe−Al−OSA were as follows: the organic phase was 30% N235 + 10% isooctyl alcohol (ROH) + 60% n-heptane, acidity of aqueous phase was about 3.00 mol/L, and phase ratio (Vo:Vw) was 8:5. More than 92.09% of Fe3+ was recovered by using countercurrent extraction process with 4−5 stages. The 99.76% of high pure Fe byproduct was obtained by stripping the loaded N235 organic phase, and it can be used as chemistry pure reagent directly. After adjusting the pH of the raffinate to 6.00 with MgO and saturated Na2CO3 solution, a...

Catalytic conversion method for preparing lower olefins and aromatics

Abstract: The invention relates to a catalytic conversion method for preparing lower olefins and aromatics. Raw oil with different cracking performances enters different reaction zones of a first riser reactor to contact with a catalytic cracking catalyst for cracking reaction to separate a spent catalyst from reaction oil gas, wherein the reaction oil gas is separated to obtain a product containing lower olefins, gasoline, distillates with distillation range of 180-250 DEG C and catalytic wax oil, wherein the gasoline is extracted by light aromatics to obtain light aromatics and gasoline raffinate; the raw materials are cracked to be sent into a second riser reactor to contract with a hot regenerated catalyst for catalytic conversion; and the spent catalysts of the two riser reactors are burned and regenerated in the same one regenerator and then returns to the two riser reactors. The method uses heavy raw materials to furthest produce the lower olefins, such as propylene, ethylene, and the like, particularly the propylene, the production rate can exceed 40 wt%, and at the same time the method can coproduce the aromatics, such as toluene, xylene, and the like.

Synergistic extraction of uranium with mixtures of PC88A and neutral oxodonors

Abstract: The extraction of uranium(VI) from nitric acid medium is investigated using 2-ethylhexyl phosphonic acid-mono-2-ethylhexyl ester (PC88A in dimeric form, H2A2) as extractant either alone or in combination with neutral extractants such as tri-n-butyl phosphate (TBP), trioctyl phosphine oxide (TOPO), and dioctyl sulfoxide (DOSO). The effects of different experimental parameters such as aqueous phase acidity (up to 10 M HNO3), nature of diluent [xylene, carbon tetrachloride (CCl4), n-dodecane and methyl iso-butyl ketone (MIBK)] and of temperature (303–333 K) on the extraction behavior of uranium were investigated. Synergistic extraction of uranium was observed between 0.5 and 6 M HNO3. Use of MIBK as diluent was also studied. Temperature variation studies using PC88A as extractant showed exothermic nature of extraction process. Studies were carried out to optimize the conditions for the recovery of uranium from the raffinate generated during the purification of uranium from nitric acid medium. Inductively Couple Plasma Atomic Emission Spectroscopy (ICP-AES) and Energy Dispersive X-Ray Fluorescence (EDXRF) techniques were employed for analysis of uranium in equilibrated samples.

Dynamic Simulation of Sorption Enhanced Reaction Processes for Biodiesel Production

Abstract: The objective of this work was to establish fixed bed sorption enhanced reactors (SER) and simulated moving bed reactors (SMBR) for the production of high purity biodiesel (fatty acid methyl ester, FAME) using esterification reactions between fatty acids (FA) in used oils and methanol. This study has demonstrated that these processes have tremendous potential in terms of overcoming the low conversion and separation difficulties that are faced in conventional biodiesel production processes. Additionally, the SMBR process operating conditions can be optimized to produce FAME at a desired purity in a continuous mode. The novelty of this work lays in the development of generic and comprehensive dynamic simulation and systematic parametric analysis frameworks. These were used to deduce the following operating conditions for achieving more than 90% conversion of FA and 80% purity of FAME, from an SMBR process: switching time of 900 s, length of 0.25 m, and feed, raffinate, and eluent flow rate ratios of 0.41, 0...

Method for removing chlorine from solution of zinc sulfate

Abstract: The invention discloses a method for chlorine from solution of zinc sulfate, which mainly comprises the following: 1, a step of extraction, in which tributylamine is used as an extractant, kerosene or para-octanol is used as diluent, clear liquid of zinc sulfate is mixed with an organic phase for extraction, and chlorine in a water phase is transferred to an organic phase; 2, a step of back extraction, in which back extraction is performed by using ammonia water or solution of sodium hydroxide, chlorine in the organic phase is retransferred to the water phase, and the organic phase is recycled; 3, a step of organic phase regeneration, in which 5 to 10 percent solution of sodium hydroxide is mixed with the organic phase which ages after being used for a certain period of time in a ratio of 1:0.9 to 1:2.5, and the mixture is stirred by an electromagnetic siterr at a high speed for 8 to 15 minutes for regenerating the organic phase; and 4, a step of deoiling, in which raffinate is subjected to active carbon absorption or ultrasonic demulsification so as to remove the organic phase in the raffinate. In the invention, the organic phase and the raffinate can be used circularly, the dechlorination rate is over 85 percent, the electrolytic operation environment is improved, the process flow is simple, and the method can be used for dechlorinating solution of zinc sulfate from wet-method zinc smelting plants and can also be used for dechlorinating wastewater.

Process for extracting rare-earth from sulfuric acid treating phosphorite process

Abstract: The invention provides a process for extracting rare earth from a sulfuric acid treating phosphorite process. In the process, a sulfuric acid refining process and a rare earth extracting process are combined, and the rare earth is reclaimed from low-concentrate sulfuric acid raffinate generated in a crude phosphoric acid extracting and refining process so as to realize reclamation of a rare-earth element. The process comprises the following steps of: (1) extracting the rare-earth element from the raffinate by adopting acidic or neutral extractant to obtain rare earth loaded organic phase and secondary raffinate; (2) washing the rare earth loaded organic phase and performing back extracting on the rare earth-loading organic phase by using acid to obtain rare earth strip liquor and blank organic phase; and (3) precipitating the rare earth strip liquor to obtain solid rare earth salt after pH value of the obtained rare earth strip liquor is adjusted, and calcining the strip liquor to obtain rare earth oxide. The process has the advantages of realizing reclamation of the rare-earth element, relatively easily extracting the rare earth, along with high rare earth extraction yield.

Method for salting out and extracting acetone and butanol from fermentation liquor

Abstract: Disclosed is a method for salting out and extracting acetone and butanol from fermentation liquor. The method is characterized by: adding one or more than two salts and one or more than two extractants to the fermentation liquor of acetone and butanol, in which salt saturation reaches 10%-100%, and the volume ratio of fermentation liquor containing the salt to the extractant is 1:0.1-1:5; and standing until phases separation to obtain an upper phase and a lower phase respectively, wherein the upper phase is a solvent or an extracting phase rich in acetone and butanol, and the lower phase is a salt-rich phase or a raffinate phase. The method has simple technology, short separating time and low separating cost, and it is therefore a method of separating acetone and butanol with promising industrial application.

Method for extracting indium and recovering valuable metals from flue dust of tin

Abstract: The invention relates to a method for extracting indium and simultaneously recovering valuable metals such as tin, lead, zinc, cadmium and the like from flue dust of smelted tin. The method comprises:adopting twice leaching: neutral leaching-acid leaching, and firstly leaching part of impurity elements such as arsenic, cadmium, zinc and the like in the flue dust of tin into the neutral leaching liquid under the condition of neutral normal temperature or low temperature; then, acidic twice leaching neutral leaching residue, leaching indium and residual part of impurity elements again, and entering high temperature leaching liquid; washing high temperature leaching residue, and then recovering tin and lead. P204 is adopted for extracting the indium in the high temperature leaching liquid, hydrochloric solution is used for back-extraction enrichment, and zinc blocks are used for replacing, so that the product sponge indium can be obtained and has the indium content of 92.70%; raffinate obtained after the indium is extracted by the P204 returns to neutral leaching or acid leaching to be taken as leaching preparation liquid; zinc in the neutral leaching liquid is extracted by P507, sulfuric acid solution is processed by back-extraction enrichment, evaporation, concentration and crystallization, so that industrial first-grade product ZnSO4.7H2O can be obtained.

Effect of Solvent Dearomatization and Operating Conditions in Steam Pyrolysis of a Heavy Feedstock

Abstract: To investigate the benefits of pretreatment in pyrolysis of heavy fractions, a feedstock in the range of gas oil has undergone aromatic extraction at different temperatures and solvent/oil ratios with n-methyl-2-pyrrolidone as the solvent. The raffinate with least aromatic content in addition to the original feed were subjected to steam cracking at different operating conditions to compare their product distributions with respect to the individual effects of temperature, flow rate, and dilution ratio. The experimental design was carried out with the use of the central composite design methodology. We find that the yields of ethylene, propylene, and butylenes increase by more than 10% upon dearomatization. The liquid products with five or more carbon atoms decrease by 13% on average. From desirable products, only butadiene reduced by about 18% upon extraction. Furthermore, a practical selectivity factor was proposed to support the preference of low residence time cracking and more generally to scrutinize t...

Method for producing granular monoammonium phosphate with raffinate

Abstract: The invention provides a method for producing granular monoammonium phosphate with raffinate, wherein, ammonia is neutralized with phosphoric acid to obtain slurry, and the slurry is concentrated and then subjected to spraying granulation to obtain the granular monoammonium phosphate. The method comprises the following steps: (1) mixing wet-process phosphoric acid with the raffinate according to a certain ratio to obtain mixed phosphoric acid, and then lowering the metal ion content in the raw material mixed phosphoric acid; and (2) adjusting the neutralization degree of neutralization reaction between the mixed phosphoric acid and the ammonia to obtain monoammonium phosphate slurry. The granular monoammonium phosphate obtained by the method can meet the requirement for nitrogen nutrients in the product, reach the product strength of no less than 40N, digest the raffinate in a wet-process phosphoric acid purification device, conform to the requirement for the current global recycling economy. The method can improve the concentration of dilute phosphoric acid, reduce steam consumption of a slurrying system, and increase the product strength of the granular monoammonium phosphate.

Method for preparing light-weight fuel oil and propylene from inferior raw oil

Abstract: The invention provides a method for preparing light-weight fuel oil and propylene from inferior raw oil. The method comprises the following steps that: the inferior raw oil enters a first and second reaction areas of a catalytic conversion reactor in sequence to contact the catalytic conversion catalyst to undergo the primary reaction and the secondary reaction, the reaction products and the spent catalyst undergo solid-liquid separation, and the spent catalyst undergoes steam stripping and singeing in sequence and then is returned to the reactor for recycling; the reaction products are separated to obtain propylene, gasoline, catalytic wax oil and other products, wherein the catalytic wax oil enters an aromatic extraction device for separation so as to obtain extract oil and raffinate oil; and the raffinate oil is cycled to the first reaction area of the catalytic conversion reactor or/and other catalytic conversion devices for further reaction to obtain the target products of propylene and gasoline. In the method, the inferior raw oil undergoes the mild catalytic conversion, the obtained catalytic wax oil undergoes aromatic extraction, and the extract oil richly contains double ring arenas and is a quite good chemically raw material; and the raffinate oil richly contains alkanes and naphthenic hydrocarbons, and is quite suitable for catalytic conversion, so that the highly efficient utilization of gasoline resources is realized.

Solvent Refining of Medium Viscosity Distillate and Changes in Group Chemical Composition

Abstract: The relative position of the phase boundary curves and changes in group chemical composition have been studied, in a single stage extraction system, with three solvents for medium viscosity, raw dewaxed lube distillate. Results obtained indicate that solvents with hydrogen-bonding tendency show low critical solution temperatures and %N + P in raffinate tends to be directly proportional to the product VI with the increase in S:F ratio. Refining effectiveness number and lube refining index together makes it possible to evaluate the solvent refining behaviour of any raw lube distillate for the desired VI level.

Simulated moving bed chromatographic separation process

Abstract: The present invention provides a chromatographic separation process for recovering a polyunsaturated fatty acid (PUFA) product, from a feed mixture, which process comprises introducing the feed mixture to a simulated or actual moving bed chromatography apparatus having a plurality of linked chromatography columns containing, as eluent, an aqueous alcohol, wherein the apparatus has a plurality of zones comprising at least a first zone and second zone, each zone having an extract stream and a raffinate stream from which liquid can be collected from said plurality of linked chromatography columns, and wherein (a) a raffinate stream containing the PUFA product together with more polar components is collected from a column in the first zone and introduced to a nonadjacent column in the second zone, and/or (b) an extract stream containing the PUFA product together with less polar components is collected from a column in the second zone and introduced to a nonadjacent column in the first zone, said PUFA product being separated from different components of the feed mixture in each zone.

Process for comprehensively and efficiently recycling zinc and indium in indium raffinate

Abstract: The invention provides a process for comprehensively and efficiently recovering zinc and indium in indium raffinate. The process adopts an iron-indium technique, adds the procedures of precipitating alum and removing iron, removes impurities, and determines a principle of returning raffinate to an electrolytic zinc system in a process of producing electrolytic zinc through wet smelting and comprehensively recovering indium. The process recycles a large amount of sulphuric acid and zinc metal in the raffinate without affecting the running of the electrolytic zinc system, and saves cost withoutpolluting environment at the same time.

Method for extracting cobalt in copper cobalt sulfide ore

Abstract: The invention provides a method for extracting cobalt in a copper cobalt sulfide ore, and relates to a method for extracting the cobalt in a copper cobalt ore which is in low grade and hard to treat and contains cobalt mineral raw materials The method is characterized by comprising the following steps: (1) crushing and grinding low sulfur containing copper cobalt ore; (2) adding water into the grinded ore material for autoclave leaching; (3) neutralizing and filtering the leached ore pulp, and sending leaching residue into tailing; (4) carrying out copper extraction, extract stripping and strip liquor electrodeposition on the filtered solution to prepare cathode copper; (5) neutralizing copper extracting raffinate to remove iron and aluminum, filter-pressing and separating the neutralized ore pulp, and performing the neutralizing step after the filter-pressed and separated residue is returned to the step (3) for leaching; (6) precipitating cobalt and nickel in filter-pressed and separated solution by adopting sodium hydroxide, wherein the separated precipitate is cobalt nickel hydroxide concentrate; and (7) returning separated after-precipitating solution to the step (2) for the leaching process The method has simple technical process and less equipment corrosion, and realizes comprehensive reclamation and utilization of valuable metals in the low sulfur containing copper cobalt concentrate

Extracting and purifying technology of high purity nickel

Abstract: The invention relates to an extracting and purifying technology of high purity nickel, mainly comprising the following steps of firstly, adding oxidant of hydrogen peroxide in nickel sulfate, adding sodium carbonate after complete reaction, producing and precipitating complex compound, and deironing by filtering; secondly, using P204 after clarifying mother solution, carrying out homogeneous saponification by using sodium hydroxide, carrying out countercurrent extraction, obtaining Cu hydrochloric acid by carrying out backextraction on an organic phase by using sulfuric acid segmentation by segmentation, and obtaining metals such as Co, Mn, Ca, Zn and the like by treating the Cu hydrochloric acid by backextraction; and thirdly, using P507 as raffinate, carrying out homogeneous saponification on the raffinate by using the sodium hydroxide, carrying out countercurrent extraction, obtaining magnesium by treating an organic phase of dilute sulfuric acid by backextraction, recovering magnesium sulfate by an aqueous phase, obtaining nickel by carrying out backextraction on the residual organic phase plus anolyte or the dilute sulfuric acid, and obtaining electronic grade nickel sulfate from the aqueous phase. The technology has the advantages of simple process, low cost and high metal yield without solid waste calcium and magnesium slag, fluoride reagent consumption and environmental pollution.