Showing papers on "Raffinate published in 1999"

Hydroconversion process for making lubricating oil basestocks

Abstract: The process is drawn to producing a lubricating oil basestock having at least 90 wt % saturates and a VI of at least 105 in unit (42) then the hydroconverted raffinate is conducted through line (46) to heat exchanger (48).

Supercritical fluid extraction of 1-butanol from aqueous solutions

Abstract: The purpose of the present work was to study the extraction of 1-butanol from aqueous solutions using supercritical carbon dioxide at 100 bar and 40°C as a solvent. Experimental studies were performed using a 35 mm diameter mechanically agitated Oldshue–Rushton-type supercritical fluid extraction column. Over 99.7% of the initial amount of 1-butanol was removed from the feed stream when the solvent-to-feed ratio was 2.7. The lowest 1-butanol concentration in the raffinate was approximately 0.02 wt%, and the extract contained typically 85–90 wt% 1-butanol. The values of the overall mass transfer coefficient Koda were in the range 0.0019–0.0034 s−1, and the values of the height equivalent to a theoretical stage HETS ranged from 0.4 to 0.5 m. Mechanical agitation had no effect on the column efficiency at the selected extraction conditions.

Supercritical CO2 extraction for utilisation of excess wine of poor quality

Abstract: Supercritical CO 2 extraction in a continuous operating high pressure extraction column has been tested for extraction of ethanol and aroma compounds out of wine, to produce a raffinate with an alcohol content of about 3 vol%. The influence of extraction parameters like pressure, phase ratio and phase contact and column packings is determined. The quality of mixtures containing the original wine and different amounts of extract was determined with the commission of a wine tester.

High temperature gas purification apparatus

Abstract: A high temperature membrane reactor or gas purification apparatus includes a housing containing a gas heating chamber and a gas extraction component, preferably one or more tubular membranes. The preferred application is for extracting hydrogen from a mixed gas flow or for generating hydrogen, e.g., by reforming methanol, ethanol, or gasoline. A surrounding annulus provides heat exchange and insulation by circulating the mixed gas flow about the housing and then injecting the mixed gas flow into the housing for extraction or reaction. The apparatus further includes an outlet for releasing raffinate preferably including a flow controlling restriction. Heating is provided by conducting the raffinate from the gas extraction component to the heating chamber wherein reaction with a catalyst generates heat. These features, alone or in combination, provide better energy management, better flow management, and better safety than current designs. A spring-type support for the membrane is further described which increases the maximum useable operation pressure of the membranes to take better advantage of the membrane reactor and gas purification features.

Rubber process oil and production process thereof

Abstract: There is described a rubber process oil in which the content of polycyclic aromatics (PCA) as determined by the IP 346 method is less than 3% by weight, which is rich in aromatic hydrocarbons, which has an aniline point of 80°C or less, and a %CA value as determined by ring analysis according to the Kurtz method of 20 to 50% The oil is produced by extraction of lube oil fractions with a solvent having a selective affinity for aromatics under conditions such that the extraction yield is regulated in dependence on the PCA content of the lube oil fraction Alternatively, the extract may be cooled to further separate it into a second extract and a second raffinate, and the second raffinate is used as the rubber process oil

Rectifying column for extractive distillation of close-boiling or azeotropic boiling mixtures

Abstract: The invention relates to a rectifying column for extractive distillation, comprising a column main section (204) and a raffinate section (205) above said main section, an evaporator (208) situated on the lower end of the column, an inlet (214) disposed between the main section of the column and the raffinate section and a solvent inlet (215) arranged on the top side of the raffinate section (205) for feeding an extracting agent. According to the invention, the main section (204) has two chambers (216, 217) connected in parallel. A stripping section (222) is disposed between the bottom of the column (221) and the main section (204), in which concentration of the extracting agent occurs from the top down. The bottom (221) is connected to the solvent inflow (215) by a device (223) for recycling the extracting agent.

Spent caustic pretreatment and enhanced oxidation process

Abstract: A process for pre-treating a spent caustic stream prior to oxidation which includes countercurrent multi-stage elevated temperature solvent extraction of dissolved organic material from the spent caustic using a solvent to yield a spent caustic raffinate containing only residual amounts of organic solute and steam distilling the spent caustic raffinate to remove the residual organic solutes, yielding a pretreated spent caustic stream substantially free of organic material which is then subjected to wet air oxidation and thereafter to ozonolysis to yield a wastewater stream having a low COD and BOD, which is neutralized to a pH of 8.5 to 9.0.

Solvent extraction of aromatic components from lube-oil cut by N-methylpyrrolidone (NMP)

Abstract: A method has been developed for the modeling of complex hydrocarbon mixtures which is based on the accurately simulated distillation gas chromatography analysis as well as the extended method of Ruzicka et al for making the model molecules. The method has been used for modeling of the complex mixture of the lube-oil cut SAE 10 in the aromatics extraction process with the solvent N-methylpyrrolidone (NMP) from the Tehran Refinery. To carry out the liquid-liquid equilibria calculations, the van der Waals surface and volume size parameters of the model molecules and NMP as well as their interaction parameters are required which they are calculated by the Bondi's group contribution method with the NMP molecule taken as a functional group according to the approach of Rahman et al. Solvent extraction process at two temperatures of 50 and 42 °C both at 1 atm have been carried out in a batch mixer-settler and the properties of resultant phases (extract and raffinate) have been determined by the precise measuring systems using the standard methods of ASTM and the well-known Riazi's equations. Finally, the results of the equilibrium calculations have been compared with the experimental data and good agreement was found.

Copper, nickel and cobalt recovery

Abstract: A process for the recovery of copper and nickel from a copper and nickel sulphide concentrate in slurry form. The slurry is subjected to a biological oxidation turning the copper sulphide to soluble copper sulphate and the nickel to nickel sulphate. The liquid containing the sulphates is separated from the slurry and treated with a solvent extraction reagent so that copper ions are exchanged by the reagent for hydrogen ions to produce a raffinate which is high in sulphuric acid and low in copper sulphate. The solvent extraction reagent is then stripped from the raffinate with a sulphuric acid solution. Copper is electrically harvested from the sulphuric acid solution and a portion of the copper depleted raffinate is returned to form a slurry with additional ore for subsequent biological oxidation. Nickel is recovered from the remaining portion of the raffinate. The preferred bacterium is at least one of Thiobacillus Ferro-oxidants, Thiobacillus Thio-oxidants, Leptospirrilum Ferro-oxidants, Thiobacillum Caldus, Acidimicrobium and Sulpholobus.

Centrifugal extraction process

Abstract: A process for extracting a component from liquids using dense phase gases or supercritical fluids (dense phase solvent). The process contacts a liquid and the dense phase solvent in a rotating mixer to dissolve a desired fraction into the dense phase solvent to form a loaded solvent. Furthermore, the mixer separates the loaded solvent from the remaining raffinate. Then the rotating mixer discharges the loaded solvent and raffinate. Decreasing pressure on the loaded solvent converts the loaded solvent into a gas and the desired fraction to liberate the desired fraction from the gas.

Modular solvent extraction plant

Abstract: A modular solvent extraction plant for extracting metal from a metal are is provided. It includes a stage-wise, plug flow contactor that mixes an aqueous solution and an organic solvent solution into a mixed emulsion, a reactor to further mix the solutions, a separator for breaking up the emulsion into an aqueous solution and an organic solution, and a loaded organic coalescer that removes aqueous entrainment. It may also include a raffinate coalescer that removes organic entrainment, a second stage-wise, plug flow contactor that mixes an electrolyte solution with the organic solution from the loaded organic coalescer to form a second mixed emulsion, a second reactor, a second separator for breaking up the second emulsion, and an electrolyte coalescer. An organic scrub station may be used in place of the loaded organic coalescer. The contactors, reactors, separators, and coalescers can be mounted on movable structures.

Process for co-production of metaxylene and paraxylene

Abstract: For co-production of metaxylene and paraxylene from a hydrocarbon feedstock in a simulated moving bed in a chromatographic column (1) that contains a number of beds 1, 2,3, 4 . . . of an adsorbent, interconnected in a loop, the column comprises an injection of the feedstock, a draw-off (14) of a first raffinate, a draw-off (17) of a second raffinate that comprises metaxylene, an injection of desorbent and a draw-off of an extract that delivers paraxylene. The injection positions and the draw-off position of the extract are offset periodically by one bed in the direction of flow of the main flux that circulates in the column. First raffinate (14) that comprises desorbent, orthoxylene, metaxylene and ethylbenzene is drawn off continuously or intermittently, and second raffinate (17) R2 that comprises orthoxylene and metaxylene is drawn off intermittently. The second raffinate is distilled in such a way as to recover orthoxylene and metaxylene separately with at least 99% purity and with an improved yield. The resultant xylenes are suitable for the production of isophthalic acid and terephthalic acid

Nicotine extraction process

Abstract: The new process for extracting nicotine includes the following steps: firstly, using hot water to extract tobacco leaf; adding Ca(OH)2 and CO2 to the extract to make neutralization; filtering to obtain the filtrate, i e refined tobacco juice; using ethyl acetate or chloroform to make extraction in filled tower; evaporating extract phase to obtain the product containing 75-85% of free nicotine; evaporating raffinate phase to recover extracting agent, so that the raffinate phase can be used as hot water for extraction, and can be cyclically used Said invention is simple in equipment, convenient in operation, does not produce waste liquid, waste gas and waste material, so that it can meet the requirements for industrial production

Rubber processing oil and its production

Abstract: PROBLEM TO BE SOLVED: To provide a rubber-processing oil that has a poor content of polycyclic aromatic compounds and a rich content of aromatic hydrocarbons. SOLUTION: This rubber-processing oil has the content of polycyclic aromatic compounds of <=3 mass % according to IP346 procedure, the aniline point of <=80 deg.C and the %CA value of 20-50% according to the Kurtz ring analysis method. This oil is obtained by solvent-extracting the deasphalted oil prepared by deasphalting the lubricant oil fraction from the vacuum distillation of crude oil or by deasphalting the stillage of the crude oil with a solvent having the selective affinity to aromatic hydrocarbon, cooling the resultant first extract and fractionating the second raffinate. Or it is obtained as an extract collected at a prescribed extraction rate, as the conditions for the solvent extraction is controlled.

Microbial Ecology Assessment of Mixed Copper Oxide/Sulfide Dump Leach Operation

Abstract: Microbial consortia composed of complex mixtures of autotrophic and heterotrophic bacteria are responsible for the dissolution of metals from sulfide minerals. Thus, an efficient copper bioleaching operation depends on the microbial ecology of the system. A microbial ecology study of a mixed oxide/sulfide copper leaching operation was conducted using an "overlay" plating technique to differentiate and identify various bacterial consortium members of the genera Thiobacillus, �Leptospirillum�, �Ferromicrobium�, and Acidiphilium. Two temperatures (30C and 45C) were used to select for mesophilic and moderately thermophilic bacteria. Cell numbers varied from 0-106 cells/g dry ore, depending on the sample location and depth. After acid curing for oxide leaching, no viable bacteria were recovered, although inoculation of cells from raffinate re-established a microbial population after three months. Due to the low pH of the operation, very few non-iron-oxidizing acidophilic heterotrophs were recovered. Moderate thermophiles were isolated from the ore samples. Pregnant liquor solutions (PLS) and raffinate both contained a diversity of bacteria. In addition, an intermittently applied waste stream that contained high levels of arsenic and fluoride was tested for toxicity. Twenty vol% waste stream in PLS killed 100% of the cells in 48 hours, indicating substantial toxicity and/or growth inhibition. The data indicate that bacteria populations can recover after acid curing, and that application of the waste stream to the dump should be avoided. Monitoring the microbial ecology of the leaching operation provided significant information that improved copper recovery.

New method of processing lupin seeds by deoiling flaked seeds, then sequential extraction with acid and alkali, useful for recovery of proteins, oil and alkaloids

Abstract: Method for treating and processing lupin seeds, containing alkaloids (I), oil and proteins, to recover products by targeted fractionation, comprises deoiling the comminuted seeds by immersion in a solvent, then treatment of the residue with acid to remove acid-soluble components, particularly (I). The seeds are comminuted and/or formed into small disk-shaped flakes, using a cooled flaking roller, after preliminary breakage of the optionally dehusked seeds. The flakes are heated indirectly to eliminate most of the water and after removal of the oil, the acid-solubles are removed by aqueous extraction to leave a raffinate of reduced (I) content and an aqueous extract.

Removal of impurities from a hydrocarbon component or fraction

Abstract: A process for removing impurities from a hydrocarbon component or fraction comprises mixing, in a liquid-liquid extraction step, an impurity-containing liquid hydrocarbon component or fraction, as an impure liquid hydrocarbon feedstock, with an acetonitrile-based solvent. Thereby, at least one impurity is extracted from the hydrocarbon component or fraction into the solvent. There is withdrawn from the extraction step, as a raffinate, purified hydrocarbon component or fraction, while there is withdrawn from the extraction step, as an extract, impurity-containing solvent.

Separation of dichlorobenzene isomer

Abstract: PURPOSE:To produce m-dichlorobenzene useful as a raw material of intermediate for agricultural chemicals, in high purity, as a raffinate component, by contacting a mixture of dichlorobenzene isomers with an X-type zeolite adsorbent containing more than a specific amount of Li cation. CONSTITUTION:A mixture containing o-, m- and p-dichlorobenzene isomers is made to contact with an X-type zeolite adsorbent containing >=60mol% (preferably >=70mol%) Li cation to obtain high-purity m-isomer as the raffinate component. The X-type zeolite is a crystalline aluminosilicate of formula (M is cation; n is atomic valence), and the cation other than Li cation is preferably Na cation. The adsorptive separation is carried out at 50-250 deg.C under atmospheric pressure - 40kg/cm G, preferably in liquid phase.

Polymerization method for styrene butadiene rubber by solution

Abstract: The synthesis of S-SBR by using n-butyl lithium or sec-butyl lithium as initiator is characterized by adding a small quantity of 2-methyl-2-hexanol potassium whose quantity is 0.025-0.367 times effective initiator in the polymerization reaction system to implement constant copolymerization of phenylethylene and butadiene in the S-SBR. Said method is applicable to the polymerization system using cyclohexane, raffinate oil and mixed solvent of cyclohexane and n-hexane as solvent, and can implement constant copolymerization in the system regardless of THF to synthesize low 1,2 structure random S-SBR, and in the final stage of the polymerization reaction it can use SnCl4 to end-cap the active tail end to form star-type S-SBR.

Sitosterol production method

Abstract: FIELD: paper-and-pulp industry. SUBSTANCE: sitosterol useful in synthesis of medicinal preparations and in food industry is prepared in a process including processing of sulfate soap or saponified tall pitch followed by isolation of neutral substances involving extraction with organic solvent in presence of water and low-molecular alcohol, extract-raffinate separation, isolating soaps from raffinate, separating betulin from extract to give concentrate of neutral substances, dissolving it in selective organic solvent, and, finely, crystallization of sitosterol. According to invention, above-said concentrate is dissolved in water-saturated methyl acetate at weight/volume ratio 1:(5-7) at 4-10 C; recrystallization of isolated sitosterol is accomplished from 85% aqueous isopropyl alcohol at 30-35 C; and sterols obtained after solvent is recovered from mother liquor are combined with above-mentioned neutral substances to be transferred into recrystallization zone. EFFECT: enabled preparation of sitosterol for synthesis of hormonal preparations with alpha-isomer content no higher than 1% and sitosterol for food industry with purity 95% and alpha- isomer content below ? %. 4 ex

The Catalytic Purification of CO-Rich Air.

Abstract: Stable heterogeneous catalysts for the oxidative removal of CO from air at ambient temperatures have been developed. An alumina support impregnated with PdCl2, CuCl2, and CuSO4 is described. Optimal activity was obtained with Pd 0.020 mol/kg, Cu 0.50 mol/kg, CuCl2 20-30% of total Cu, a 2- to 24-hr soak, filtration of surplus raffinate, and a 2- to 4-hr firing in air at 200-350 °C. The catalysts are effective at 20-26 °C and relative humidities in the 15-90% range. They are reversibly deactivated by completely dry or water-saturated air streams. These catalysts have been tested at space velocities up to 30,000 hr-1. In contact with 25 sec-1). At much higher CO concentrations, the maximum CO loading rate-limited by the Cu(I) reoxidation rate-is approximately 17 m mol CO per Limol Pd per hour.

Recovery of Dimethylnaphthalene Isomers from Light Cycle Oil by O/W/O Emulsion Liquid Membrane Process

Abstract: This paper simulates a process for recovering dimethylnaphthalene isomers (DMN) from light cycle oil (LCO), a by-product in cracked gasoline manufacture. The process involves a multistage emulsion liquid membrane permeator for separating aromatics from paraffins in LCO and four distillation towers of which two towers are used to recover solvent from raffinate and permeate and the others are used to separate DMN from other aromatics in permeate. Stirred vessels are employed as contactors. Prior to the simulation, a series of continuous experiments on emulsion liquid membrane permeation were conducted to collect permeation coefficient data. The permeation coefficient data obtained was thereafter used to develop an empirical correlation needed for the simulation. During the simulation, the effects of permeator variables on the energy demands of the distillation towers and on the yield of DMN were investigated at a fixed DMN concentration in the product. The permeator variables studied included solvent-to-feed ratio, stirring rate, number of stages, permeator reflux ratio, and stage volume, as well as the kinds of solvents. DMN yield increased with stirring rate, number of stages, and stage volume, decreasing with permeator reflux ratio, and not affected significantly with solvent-to-feed ratio. The lighter the solvent, the lower were the energy demand and DMN yield. In the conditions of the study, about 80% of DMN in LCO could be recovered. Most of the energy consumed was used to recover the solvent. A quick analysis showed that the energy demands might be met by utilizing the raffinate obtained.

Pseude moving bed type separating device

Abstract: PROBLEM TO BE SOLVED: To clean a circulating fluid passage for a short time by introducing a cleaning liquid from one end part of a packed bed to clean the packed bed. SOLUTION: In the case of cleaning, for example a column (a), a t first, a pump P and PF are stopped. And a solenoid valve VDa and a solenoid valve VEa or VRa are opened and the other solenoid valves are closed. Next, a pump PD so started and the cleaning liquid is supplied to the column (a) through an eluant supply line D and an eluant introducing line and is drawn from an extract drawing line Ea or a raffinate drawing line Ra . It is judged that the cleaning of the column (a) is finished when the concentration of a strong absorption component or a weak absorption component becomes equal to or below a prescribed value in a strong absorption component concentration monitor EM provided in an extract integrated drawing line or a weak absorption component concentration monitor ER provided in a raffinate integrated drawing line R.