Showing papers on "Raffinate published in 2009"

Demonstration of a SANEX process in centrifugal contactors using the CyMe4-BTBP molecule on a genuine fuel solution

Abstract: Efficient recovery of minor actinides from a genuine spent fuel solution has been successfully demonstrated by the CyMe4‐BTBP/DMDOHEMA extractant mixture dissolved in octanol. The continuous countercurrent process, in which actinides(III) were separated from lanthanides(III), was carried out in laboratory centrifugal contactors using an optimized flow‐sheet involving a total of 16 stages. The process was divided into 9 stages for extraction from a 2 M nitric acid feed solution, 3 stages for lanthanide scrubbing, and 4 stages for actinide back‐extraction. Excellent feed decontamination factors for Am (7000) and Cm (1000) were obtained and the recoveries of these elements were higher than 99.9%. More than 99.9% of the lanthanides were directed to the raffinate except Gd for which 0.32% was recovered in the product.

Separation of D‐psicose and D‐fructose using simulated moving bed chromatography

Abstract: Simulated moving bed (SMB) processes have been widely used in the sugar industries with ion-exchange resin as a stationary phase. D-Psicose, a rare monosaccharide known as a valuable pharmaceutical substrate, was synthesized by the enzymatic conversion from D-fructose. The SMB process was adopted to separate D-psicose from D-fructose. Before the SMB experiment, the reaction mixture including D-psicose and D-fructose was treated by a deashing process to remove contaminants, such as buffers, proteins, and other organic materials. Four columns packed with Dowex 50WX4-Ca2+ (200–400 mesh) ion-exchange resins were used in the four-zone SMB. Single-step frontal analysis was performed to estimate the isotherm parameters of each monosaccharide. The operating conditions of the SMB process were determined based on the Equilibrium Theory. According to the simulation of the SMB process, the purity and yield of extract product (D-psicose) achieved were 99.04 and 97.46%, respectively and those of raffinate product (D-fructose) were 99.06 and 99.53%, respectively. Under the optimized operating condition, complete separation (extract purity = 99.36%, raffinate purity = 99.67%) was achieved experimentally.

Production of phytosterol esters from soybean oil deodorizer distillates.

Abstract: Enzymatic esterification and supercritical fluid extraction was used to produce phytosterol esters from soybean oil deodorizer distillates. The raw material was first subjected to a two-step enzymatic reaction; the product obtained mainly comprised fatty acid ethyl esters, tocopherols and phytosterol esters, together with minor amounts of squalene, free fatty acids, free sterols and triacylglycerols. The phytosterol esters were then purified from this mixture using supercritical carbon dioxide. Experimental extractions were carried out in an isothermal countercurrent column (without reflux), with pressures ranging from 200 to 280 bar, temperatures of 45-55 °C and solvent-to-feed ratios from 15 to 35 kg/kg. Using these extraction conditions, the fatty acid esters were completely extracted and, thus, the fractionation of tocopherols and phytosterol esters was studied. At 250 bar, 55 °C and a solvent-to-feed ratio of 35, the phytosterol esters were concentrated in the raffinate up to 82.4 wt-% with satisfactory yield (72%).

Naphtha fecundation aromatic hydrocarbons reforming system

Abstract: The utility model discloses a Naphtha prolific arene reforming system, and the system comprises a heating device and reaction devices; and is characterized in that: the reaction devices are connected with a high pressure separator; the high pressure separator is connected with a stabilization system; the lower part of the stabilization system is connected with an extraction system by a pipeline; the extraction system is connected with a raffinate oil cutting system by a pipeline on the one hand; the middle part of the raffinate oil cutting system is connected with the other reaction device by a pipeline and a heating device, the lower part of the raffinate oil cutting device extracts coal oil through the pipeline; and the other end of the other reaction device is connected with the high pressure separator by a pipeline The utility model has the advantages of greatly increased processing capacity, liquid yield, arene yield and hydrogen output

Solvent extraction of uranium from acidic sulfate media by Alamine® 336: computer simulation and optimization of the flow‐sheets

Abstract: BACKGROUND: A series of nine conventional and non-conventional flow-sheets have been considered for the recovery of uranium from acidic sulfate solution by liquid–liquid extraction with 0.146 mol L−1 Alamine® 336 in kerosene modified with 5% w/w 1-tridecanol and stripping with a 199 g L−1 Na2CO3 solution. The reference flow-sheet was a classical counter-current configuration with four mixers–settlers in the extraction stage and three mixers–settlers in the stripping stage. The others flow-sheets possessing a total of eight mixers–settlers are unusual combined solvent extraction flow-sheets with one or two independent extraction stripping loops and with one or two feed inlets. RESULTS: The configuration of the flow-sheets strongly influences the extraction performance of the process depending on the working conditions (feed, stripping and solvent flow rates). The presence of two independent extraction–stripping loops may allow the delay of the saturation phenomenon encountered in the conventional flow-sheet and thus, to operate at higher feed flow rates without loss of performance, as far as the residual fraction in the raffinate and the concentration factor in the stripping solution are concerned. Furthermore, the presence of a modification in the non-conventional flow-sheets with two independent extraction–stripping loops and two feed inlets leads to interesting configurations for uranium recovery from less concentrated solutions, such as heap leach solutions. CONCLUSION: The use of non-conventional flow-sheets is interesting as it allows the process of uranium (VI) recovery by liquid–liquid extraction to be improved. Copyright © 2009 Society of Chemical Industry

Dyeing residual liquid recycling and dye recovery processing method, and special dyeing residual liquid processing pool

Abstract: The invention relates to a method for reusing dyeing raffinate of cellulosic fiber dye, recovering and treating dye, as well as a structure of a special dyeing raffinate treatment pond. According to different dyeing methods and different application categories of dyes, typical basic dyes are selected, and the maximum absorption wavelength or characteristic wavelength of each basic dye is sought so as to determine the content of each blended dye in raffinate and reuse the raffinate in production, while the dyeing raffinate which cannot be directly used in production is recovered through a special treatment pond and a corresponding method. The invention solves the technical problems that the prior art cannot directly reuse the dyeing raffinate in production, cannot recover the dyes in the dyeing raffinate, and has no special treatment device and equipment for recovering and reusing the dyes.

Method of preparing high pure cathode copper by using PCB acid chlorine copper etching solution sewage

Abstract: The present invention disclose a method of preparing high pure cathode copper by using PCB acid chlorine copper etching solution sewage, the main technical characteristics include applying sewage preprocess procedure to satisfy extraction need better, programming multi-extraction to improve extraction recovery rate of cooper, applying extractant with high selectivity avoid extraction entrainment design, washing procedure etc. to reduce carried impurity and dispel affect of chloride ion to electrodeposition. The electrodeposition applies additive to improve copper crystallinity, simultaneity, utilize residual useful ingredient in raffinate to prepare copper etching solution, arriving the objective of both prepare high pure cathode copper effectively and regenerative cycle use of the etching solution. The purity of the prepared cathode copper reaches 99.99%.

Simulated countercurrent adsorptive separation process

Abstract: A process is described for the separation of a first chemical compound from a liquid feed stream comprising at least first and second chemical compounds by simulated countercurrent adsorptive separation. In the process, the feed stream and a liquid desorbent stream are passed into at least one multi-bed adsorbent chamber at two different points via different transfer lines and an extract stream rich in the first chemical compound and a raffinate stream depleted in the first chemical compound are removed from the adsorbent chamber at two different points by two additional transfer lines. In addition, the contents of the transfer line which has just been used to supply the desorbent stream are flushed into the adsorbent chamber at a point along the chamber between the transfer line just used to supply the desorbent stream and the transfer line just used to withdraw the raffinate.

Method for extracting residual oil and tea saponin from tea seed cake after oil extraction

Abstract: The invention relates to a method for extracting raffinate oil and tea saponin from tea seed cake after oil extraction, which belongs to the field of grain and oil processing and byproduct extracting techniques. The technique of the invention mainly comprises the processes: after the extracted tea seek cake is crashed and dried, the raffinate oil is extracted by using industrial hexane or sherwood oil, the extracted raffinate oil is distilled to remove the solvent so as to obtain crude oil; the distilled solvent can be recycled, the tea seed cake after the raffinate oil is adopted to leach tea saponin by 85 to 95 percent ethanol, the tea saponin is subjected to the water bath heat and reflux for 2 to 3 hours at a temperature of between 70 and 80 DEG C, the tea saponin concentrated solution is obtained after filtering, distilling and concentrating processes, the depigmentation treatment is performed by using active carbon or 35 percent H2O2, and certain mount of acetone is added to the processed solution to keep stand for 1 to 2 hours; and after the tea saponin separates out completely, and the product of tea saponin is obtained by filtering and drying processes.

Process for converting inferior feedstock to high quality fuel oil

Abstract: A catalytic conversion process can convert inferior feedstock to high quality fuel oil and propylene. A inferior feedstock is introduced into first and second reactor zone, wherein the feedstock carry out first step and second step reactions by contacting with catalytic conversion catalyst. Product vapors separate from spent catalyst by gas-solid separation. The spent catalyst is stripped, regenerated by burning off coke and then returns to reactor. The product vapors are introduced into separation system to obtain propylene, gasoline, diesel, fluid catalytic cracking gas oil (FGO) and other products. The FGO is introduced into hydrotreating unit and/or extraction unit to obtain hydrotreated FGO and/or extracted FGO. Said hyrotreated FGO and/or extracted FGO return to the first reactor zone and/or another catalytic cracking unit to obtain propylene and gasoline. The extracted oil of said FGO is rich in double ring aromatics which are good chemical materials. The raffinate of said FGO is rich in chain alkane and cycloalkane which are suitable for catalytic cracking. More particularly, the invention relates to a process to utilize petroleum oil resources efficiently for decreasing the yield of dry gas and coke significantly.

Counter-Current Carbon Dioxide Purification of Partially Deacylated Sunflower Oil

Abstract: A liquid carbon dioxide counter-current fractionation method was developed to remove by-product fatty acid propyl esters (FAPEs) from the reaction mixture after the partial deacylation of sunflower oil. The fractionation column was 1.2 m long and separations were done at 25 °C and 8.27 MPa. Several solvent to feed ratios (S:FR) (i.e., 7.6, 15.2, 30.3 and 60.6 g/g) and feed rates (FR) (i.e., 1, 2, 2.5, 3 and 4 mL/min) at a constant S:FR of 15.2 were examined. Raffinate purity (i.e., percentage glycerides) and extract purity (i.e., percentage FAPEs) were both monitored. Percentage glycerides in both the raffinate and the extract increased with S:FR. The raffinate contained ca. 83, 97, 100 and 100% glycerides at S:FRs of 7.6, 15.2, 30.3 and 60.6, respectively. The percentage glycerides in the extracts were ca. 3, 4, 8 and 17%, respectively. With the S:FR held constant at 15.2, the raffinate purity peaked at ca. 99% glycerides at a FR of 2.5 mL/min and the extract at this FR contained ca. 96% FAPEs. The optimal S:FR and FR determined from the experimental assays was applied to large batches in both a semi-continuous feed mode, and later in a continuous feed mode, which gave raffinates of 99.3 and 98.1% glycerides, respectively, and extracts of 97.3 and 97.2% FAPEs, respectively.

Method for acid leaching extraction of vanadium from vanadium-containing raw material

Abstract: The invention relates to a method for extracting vanadium(V) from vanadium-containing materials, in particular to a method for acid-leaching vanadium from the vanadium-containing materials. The method comprises the following steps: a. adding water to the vanadium-containing materials and evenly stirring; gradually adding sulfuric acid with the mass fraction being 20% to 60% to adjust the pH value of the acid-leaching reaction system to 2.5 to 3.3; and filtering to obtain residue and acid-leaching solution upon completion of acid-leaching; and b. leaching vanadium from the acid-leaching solution obtained in Step a with SO4 type anion exchange resin by ion-exchange. The method can effectively prevent ions, such as Fe, Mg, Al, Mn, P, Cr and the like, in the vanadium-containing materials from entering the acid-leaching solution during acid-leaching process and greatly reduce the pressure on the subsequent purification of the acid-leaching solution; and the ion-exchange raffinate can be recycled in the acid-leaching step, thereby increasing the overall recovery rate of vanadium and avoiding problems in environmental pollution caused by discharging a large quantity of vanadium-leaching waste water.

Method for recovering dilute acetic acid by extraction and azeotropic distillation

Abstract: The invention provides a method for recovering dilute acetic acid by extraction and azeotropic distillation. An extraction tower is additionally arranged on the basis of an azeotropic rectification tower and a solvent recovery tower; the dilute acetic acid is transmitted to the top of the extraction tower; a small fraction of the top backflow of the azeotropic rectification is transmitted to the bottom of the extraction tower as the extractant to carry out counter current contact extraction with the dilute acetic acid at normal temperature, wherein the volume ratio of the two flows is 1:(1-5); the extraction rate of the extraction tower is equal to or larger than 95%; the extraction phase as well as the other fraction of an entrainer enters the azeotropic rectification tower and is concentrated; and the raffinate phase enters the solvent recovery tower to further.

Value Addition to Sulfate Waste Pickle Liquor of Steel Industry Using Hydrometallurgical Processes

Abstract: The solvent extraction of concentrated acid was investigated from sulfate waste pickle liquors using Cyanex 923 (trialkylphosphine oxide (TRPO); manufactured by Cytec Industries Inc., Woodland Park, NJ; provided by Cyanamid Canada Inc. (Markham, Canada)) as an extractant. The effect of various parameters was studied such as extractant concentration, organic-to-aqueous phase ratio, temperature. and retention time on acid extraction from the waste pickle liquor to the organic phase, After the saturation of the organic phase with sulfuric acid, stripping studies were performed to back-extract the pure acid into the aqueous phase. The raffinate of the solvent extraction process that contains both ferrous and ferric iron as well as trace impurities was subjected to oxidation and hydrothermal treatment to precipitate iron with a well-defined pseudo-cubic morphology and a high coercivity value that renders it suitable for high-grade ferrite production.

Wet-smelting method of copper and zinc bulk concentrate

Abstract: The invention discloses a wet-method smelting method for copper-zinc bulk concentrate, which comprises the following steps: refractory low-grade copper-zinc bulk concentrate is subjected to sulfurization roasting first, and flue gas is recovered and used for preparing a sulfuric acid; roasted residue is leached out in a pickling tank; leached pulp is subjected to thickening and washing to obtain coarse feed liquid for standby; thickened underflow is subjected to filtration and washing to obtain filtrate, and filter residue is recovered; the coarse feed liquid and the filtrate are subjected to fine filtration to obtain fine filtrate; raffinate obtained by extracting the fine filtrate by an extractant A is used for recovering zinc, and extract is sent to an electrodeposition workshop section, and subjected to back-extraction to obtain a copper-rich electrolyte; an insoluble anode electrodeposition method is adopted to obtain cathode copper; copper raffinate is neutralized by alkaline until the pH value is between 3 and 6 and subjected to impurity removal, and extracted by an extractant B to obtain zinc extract; the zinc extract is subjected to back-extraction to obtain zinc-rich electrolyte; and the insoluble anode electrodeposition method is adopted to obtain cathode zinc. The method recovers useful elements in the ores with low cost and high quality, namely not only recovering the copper with high yield but also recovering the zinc with high yield, avoids resource waste, greatly improves the surrounding environment, and eliminates zinc pollution.

Process and device for separation in a simulated moving bed with a bypass fluid flow rate that is not regulated automatically

Abstract: Process for separation of a feedstock F by adsorption in a simulated moving bed in an SMB device that comprises a zone 1 for desorption of compounds produced by extraction, a zone 2 for desorption of compounds produced with a raffinate, a zone 3 for adsorption of compounds produced by extraction, and a zone 4 that is located between the draw-off of the raffinate and the supply of the desorbent, whereby the device comprises external bypass lines L i/i+1 directly joining two successive plates P i , P i+ , that are equipped with non-automated means for adjusting flow rate and closing means, in which the degree of opening of the restriction means of the scavenging flow rate of the bypass lines L i/i+1 is adjusted so as to obtain the best performance of the SMB.

Processing of manganese nodule leach liquor for the separation of cobalt and nickel using PC 88A

Abstract: The SO2-ammoniacal ammonium sulfate leach liquor generated by leaching of manganese nodules, after removal of minor quantities of iron and manganese, contained copper, nickel, cobalt, zinc and (NH4)2SO4. After extraction of copper from the leach liquor with LIX 84I, stripping of ammonia from the Cu-barren raffinate was carried out followed by precipitation of metal ions from the ammonia-stripped solution as sulfides. Leaching of the sulfide precipitate was carried out with H2SO4 to obtain a leach liquor containing 0.58 kg/m3 Cu, 2.67 kg/m3 Zn, 2.00 kg/m3 Co, 24.68 kg/m3 Ni and 10.0 kg/m3 (NH4)2SO4. After extraction of copper and zinc from the sulfate leach liquor with LIX 84I and D2EHPA, respectively, the solution was left with Co and Ni. Extraction of cobalt from the Cu- and Zn-free solution was carried out with 0.1 M PC88A and stripping of the cobalt-loaded organic was carried out with the cobalt-spent electrolyte (pH 1.4). Extraction of nickel from the cobalt-free solution was carried out with 90% neutral 1M NaPC88A followed by stripping of the nickel-loaded organic with 120 kg/m3 H2SO4 solution. Extraction of metal ions increased with increasing equilibrium pH and extractant concentration. The maximum separation factors, with respect to the pH and extractant concentration variation studies, were 3796.7 and 15350.0, respectively. The extracted species for the metal ions were CoA2⊙3HA and NiA2⊙5HA.

A fast and sensitive method for the determination of uranium in the Thorex Process streams

Abstract: This paper presents a simple, rapid and sensitive radiometric method for the determination of uranium in Thorex Process stream containing large amount of thorium. This method involves the extraction of uranium into 0.05M tri-n-octyl phosphine oxide (TOPO) in xylene at 2M HNO3. The extraction of thorium is prevented by masking them with suitable quantity of fluoride ions. The optimum experimental parameters for extraction of 233U were evaluated and using the most suitable experimental conditions the extracted uranium is radiometrically determined by α-counting in proportional counter with a prior knowledge of specific activity of uranium. Simultaneously in the same sample uranium was determined by spectrophotometric method using 2-(5bromo-2 pyridylazo)-5-diethylaminophenol (Bromo-PADAP) as chromogenic reagents. Simulated as well as actual samples of dissolver, conditioner and raffinate tank of Thorex stream have been analyzed by both these methods. The method was tested for as low as 0.15 μg of uranium and the results of these analyses were found to be satisfactory within the experimental limits.

Method for continuously recycling solvent-flux for industrially compounding PPTA

Abstract: The invention relates to a method for recycling a solvent-flux for industrially compounding PPTA, comprising the following steps: (1) a mother solution which comprises NMP solvent, salt, water and trace oligomer and is obtained after synthetic PPTA resin is washed by water is extracted and separated to respectively obtain an extract phase NMP-extractant system and a raffinate phase salt-water-extractant system; (2) water obtained after an raffinate phase is stripped and separated is used for washing the resin, and the obtained extractant is recycled; (3) water obtained after an extract phase is rectified and delaminated is used for washing the resin, the obtained extractant is recycled, and coarse NMP obtained through separation is recycled after being purified By extraction for desalination, the method solves the problem that NMP is thermally cracked under the condition of salt existence because the salty mother solution is directly distilled, largely enhances the solvent recovery rate (reaching above 97 percent), has low energy consumption, and recycles the flux simultaneously, such as calcium chloride The method can realize closed, continuous and clean production and is beneficial to protecting the environment