Showing papers on "Raffinate published in 1985"

Upgrading shale oil by a combination process

Abstract: A method for reducing the nitrogen content of shale oil is disclosed. The method comprises distilling shale oil to form a distillate containing lighter shale oil compounds and a residue containing heavier compounds. Nitrogen-containing compounds are extracted from the distillate to form a first nitrogen-lean raffinate and a first nitrogen-rich extract. Nitrogen-containing compounds are also extracted from the residue to form a second nitrogen-lean raffinate and a second nitrogen-rich extract. The second nitrogen-lean raffinate is hydro-treated to further reduce its nitrogen content.

Process for metal recovery from steel plant dust

Abstract: A process is provided for hydrometallurgical processing of steel plant dusts containing cadmium, lead, zinc, and iron values, along with impurities such as chloride and fluoride salts of sodium, potassium, magnesium, etc. The first step in the process involves leaching the dust in a mixed sulfate-chloride medium that dissolves most of the zinc and cadmium. Any iron and aluminum dissolved in this step is precipitated by oxidation and neutralization. Zinc is recovered from the resulting solution by solvent extraction which provides a raffinate which is recycled to the leaching step with a bleed stream also provided for recovery of cadmium and removal of other impurities from the circuit. The lead sulfate residue from the leaching step is leached with caustic soda, and zinc dust is used to cement the lead out from the caustic solution, which then joins the main solution for zinc recovery. The residue from the lead leaching step is mixed with iron-aluminum oxide precipitate and agglomerated into pellets using cement. These pellets can be charged into steel furnaces for iron recovery or stored as a nontoxic waste.

Extraction and Recovery of Plutonium and Americium from Nitric Acid Waste Solutions by the TRUEX Process : Continuing Development Studies

Abstract: This report summarizes the work done to date on the application of the TRUEX solvent extraction process for removing and separately recovering plutonium and americium from a nitric acid waste solution containing these elements, uranium, and a complement of inert metal ions. This simulated waste stream is typical of a raffinate from a tributyl phosphate (TBP)-based solvent extraction process for removing uranium and plutonium from dissolved plutonium-containing metallurgical scrap. The TRUEX process solvent in these experiments was a solution of TBP and octyl(phenyl)-N,N-diisobutylcarbamoylmethylphosphine oxide (CMPO) dissolved in carbon tetrachloride. A flowsheet was designed on the basis of measured batch distribution ratios to reduce the TRU content of the solidified raffinate to less than or equal to 10 nCi/g and was tested in a countercurrent experiment performed in a 14-stage Argonne-model centrifugal contractor. The process solvent was recycled without cleanup. An unexpectedly high evaporative loss of CCl4 resulted in concentration of the active extractant, CMPO, to nearly 0.30M in the solvent. Results are consistent with this higher CMPO concentration. The raffinate contained only 2 nCi/g of TRU, but the higher CMPO concentration resulted in reduced effectiveness in the stripping of americium from the solvent. Conditions can be easily adjusted to give high yields and good separation of americium and plutonium. Experimental studies of the hydrolytic and gamma-radiolytic degradation of the TRUEX-CCl4 showed that solvent degradation would be (1) minimal for a year of processing this typical feed, which contained no fission products, and (2) could be explained almost entirely by hydrolytic and radiolytic damage to TBP. Even for gross amounts of solvent damage, scrubbing with aqueous sodium carbonate solution restored the original americium extraction and stripping capability of the solvent.

Process for separating monoterpenes

Abstract: An adsorptive method of separating alcohols and aldehydes or ketones and alcohols of monoterpenes is disclosed. The method uses an X-type zeolite containing sodium and potassium cations to selectively adsorb the alcohols thereby allowing recovery of an aldehyde or ketone raffinate stream and, after desorption, an alcohol extract stream. The method is suitable for feed mixtures containing individual or multiple monoterpenoid components.

Method for the separation of aromates from hydrocarbon mixtures containing aromatics

Abstract: A method is disclosed for the separation of aromates from hydrocarbon mixtures employed as entry products, by means of extractive distillation, employing as selective solvent N-substituted morpholine, the substitutions of which display no more than 7 C atoms. The raffinate produced as top product of the extractive distillation is subjected to a distillation, whereby the produced sump product with a solvent content between 20-75% by weight and a temperature between 20°-70° C., is led into a separation container and there separated into a heavy and a light phase. The heavy phase is then recycled into the extractive distillation column, whereas the light phase is recycled into the raffinate distillation column.

Single phase clear liquid after-shave treatment product containing aloe vera

Abstract: Described is a single phase clear hydroalcoholic after-shave treatment product containing aloe vera and, optionally, allantoin and a process for preparing same comprising the steps of: (a) either forming: (i) aloe vera gel; or (ii) a product resulting from steam distilling aloe vera leaves and separating the resulting oil phase from the resulting aqueous phase; (b) extracting the oil-miscible aloe vera fraction from the organic phase of the steam distillation product or from the aloe vera gel by intimately admixing therewith a quantity of extraction solvent and physically separating the extract phase from the raffinate phase; (c) separating the extraction solvent from the oil-miscible aloe vera extract phase by means of fractional distillation; (d) intimately admixing the resulting distilled oil-miscible aloe vera phase with a totally miscible perfume oil; (e) admixing the resulting mixture with a polyalkylene glycol, a polyalkylene glycol alkyl ether, a quaternary ammonium salt, a lanolin oil-polyalkylene glycol reaction product, water and, optionally, allantoin or an allantoin-aluminate complex, with the amount of water being in the range of from about 30% up to about 50% by weight of the total mixture.

Process for separation of coal tars

Abstract: Coal tars are separated, by treatment with supercritical gases, into an oil fraction and a solid-free pitch. The starting tars are treated with the compressed gases in two stages; in the first stage, the tars are saturated with the gas and freed from solid contaminants by filtration or centrifuging, and in the second stage the tars are extracted with further quantities of compressed gas. The resulting extract is converted, by changing the temperature and/or the pressure, into an oil fraction, and the raffinate obtained is converted, by pressure release, to a solid-free pitch.

Recovery of sulfolane

Abstract: RECOVERY OF SULFOLANE ABSTRACT I In a process for the production of t-butylstyrene by oxydehydrogenation of t-butylethylbenzane, sulfolane solvent employed in the preparation of purified t-butylstyrene product is recovered for recycle by extraction of aqueous sulfolane with a liquid aliphatic or aromatic hydrocarbon having a boiling point less than the boiling point of sulfolane. The raffinate is then distilled to recover sulfolane containing only small quantities of water and substantially free of organic contaminants. BACKGROUND OF THE INVENTION The invention relates broadly to a solvent recovery process and in particular to the recovery of sulfolane used in the purification of t-butylstyrene. Tertiary-butylstyrene (tBS) is a compound which is advantageously prepared by catalytic oxydehydrogenation of t-butylethylbenzene (tBEB). It has many uses, e.g. as a chemical intermediate, as a monomer or comonomer in the production of polymeric materials and the like. Tertiary-butylstyrene has often replaced styrene in some applications because desirable physical and chemical product properties result from such a substitution. In addition, there are processes where styrene is not suitable but where tertiary-butylstyrene functions well. Because tBS belongs to the same family as styrene, there are similarities in the chemistry. One of the common properties is the tendency for the styrenics to polymerize whenever they are activated by chemicals or by heat. Some of the techniques used in purifying styrene can be used to purify tBS. However, because the boiling point of tBS is about 70°C higher than that of styrene, the tendency for tBS to polymerize is much greater than that of styrene in any of the commercial processes for purifying styrene. Some of the differences between styrene and tBS are derived from the compounds of the dialkenylbenzene family, that are present in tBS but not in styrene. These crosslinking compounds can polymerize to give a type of

Separation of specific component in pseudo-moving bed

Abstract: PURPOSE: To reduce the number of adsorption tower in the conventional pseudo- moving bed, by removing a group of adsorption towers between an outflow position of raffinate liq. and an inflow position of an eluting liq. to intercept the flow therebetween, and flowing an eluting liq. CONSTITUTION: A row liq. is flowed into a port of an adsorption tower C 1 through a valve FV 12 . While a component A in the raw liq. is selectively adsorbed on an adsorbent, substantially no component B is adsorbed and advanced to the down stream, and a raffinate liq. of the component B liq. is flowed out of a valve DV 4 . Only a shutoff valve V 4 between an adsorption towers C 4 and C 5 is closed, and an eluting liq. is flowed in through a valve FV 4 . In this way, the component. A adsorbed on the adsorbent is eluted, and a product liq, rich in the component A is flowed out of a valve DV 8 at the bottom of an adsorption tower C 8 . After a predetermined period of time, the operation is stopped, and an inflow point of the raw liq. is switched to a valve FV 1 , an outflow point of the raffinate liq. to a valve DV 5 , the shutoff valve to a V 5 , an inflow point of the eluting liq. to a valve FV 5 , and an outflow point of the product liq. to a DV 9 , and succesively shifting down afterward. COPYRIGHT: (C)1987,JPO&Japio

Process for continuously preparing alkanolamin and/or alkylamin photosulfonates from fatty esters or petroleum paraffins, and alkanolamin and/or alkylamin photosulfonates so obtained

Abstract: of EP00803881. Process for the continuous preparation of alkanolamine and/or alkylamine photosulphonates from a starting material (1) constituted by fatty acid methyl esters or petroleum paraffins comprising the following steps : a) submitting the said starting material (1) to photosulphonation under anhydrous conditions by a mixture (3) of sulphurous anhydride and oxygen under ultraviolet irradiation ; b) degassifying the product (4) from stage a of the sulphurous anhydride which it contains ; the process being characterised in that it comprises in addition the following stages ; c) adding to the degassified product (8) obtained from stage b an amount of alkanolamine and/or alkylamine (10) greater than that strictly necessary for the neutralisation of the sulphonic acids contained in such a way as to separate the mixture thus obtained into two phases, a lighter phase called the raffinate (11) and a heavier phase called the extract (12) ; d) recycling to stage a the said raffinate (11) which contains unsulphonated starting material (1) ; e) recovering the said extract (12) which contains the alkanolamine and/or alkylamine polysulphonates.

Process for separating ketoses from alkaline- or pyridine-catalyzed isomerization products

Abstract: A process for the liquid phase adsorptive separation of psicose from an aqueous feed mixture of monosaccharides containing psicose along with other aldoses and ketoses. The feed is contacted with a calcium-Y type zeolite in two stages. In the first, psicose and fructose are selectively adsorbed to the substantial exclusion of other aldoses and ketoses. In the second, psicose is adsorbed to the substantial exclusion of fructose, which is recovered in high purity in the raffinate. The process can be carried out on a commercial scale by means of a simulated moving bed flow scheme.

Separation of 3,5-dichlorotoluene

Abstract: PURPOSE:To separate and recover the objective compound as a raffinate component, in high efficiency, in the adsorptive separation and recovery of the titled compound useful as an intermediate of novel agricultural chemical from the mixture of its isomers, by using a faujasite-type zeolite adsorbent. CONSTITUTION:3,5-Dichlorotoluene (3,5-DCT) is separated and recovered by adsorption process, from the mixture of DCT isomers containing 3,5-DCT and obtained by the isomerization of a mixture of DCT isomers under isomerization reaction condition. In the above process, the objective compound can be separated and recovered from the DCT isomer mixture containing 2,4-, 2,5- and/or 2,6- DCT having nearly equal boiling point to that of the objective compound by using a faujasite-type zeolite adsorbent of formula [M is cation, especially the I A, I B,IIA group of the periodic table, T1, proton or ammonium; n is atomic valence of M; x is 2.5+ or -0.5 (X-type) or 3-6 (Y-type); y depends upon the degree of hydration].

Process for preparing sulfonated triaryl phosphines

Abstract: not available for EP0104967Abstract of corresponding document: US4483801Sulfonated triarylphosphines well suited for catalysis are facilely prepared by (i) sulfonating the aromatic moieties of a corresponding triarylphosphine starting material with an H2SO4/SO3 mixture; (ii) hydrolyzing the sulfonation reaction mixture to terminate said sulfonation reaction when same has attained the desired degree of sulfonation, thereby producing a hydrolysate rich in sulfuric acid and which comprises the product sulfonated triarylphosphine; (iii) next liquid/liquid extracting said hydrolysate with an organic phase comprising at least one phosphoric or diphosphoric, phosphonic or diphosphonic, phosphinic or diphosphinic ester, or phosphine oxide or diphosphine dioxide, or slightly water miscible or immiscible C4-C12 alcohol, or sulfoxide extractant, whereby the sulfonated triarylphosphine is extracted into said organic phase, (iv) separating the organic phase from the aqueous raffinate; (v) regenerating said organic phase with water or with an aqueous solution; and (vi) recovering an aqueous solution of said sulfonated triarylphosphine.

Preparation of base lubricating oil with low pour point

Abstract: PURPOSE:To prepare a base lubricating oil having a low pour point, under mild conditions and persistent catalyst activity, by using a specified binderless crystalline aluminosilicate as catalyst in the production of base lubricating oil by catalytic dewaxing of raffinate. CONSTITUTION:Used as caralyst is a binderless rystalline aluminosilicate, pref. metal-contg. hydrogen type ISZ zeolite in pellets having a particle diameter of about 1.5mm., which gives an X-ray diffraction pattern of substantially crystalline aluminosilicate showing a single diffraction curve when 2theta is 14.7 deg. and clearly separated diffraction curves at 2theta=23 deg. and 2theta=23.3 deg.. A hydrocarbon oil (having a boling point of about 250-650 deg.C) obtained by treating a distillate oil fraction of paraffinic crude oil with a selective solvent for aromatic hydrocarbon and hydrogen are made to interact in the presence of the above catalyst.

Lubricants, in particular for lubricating tools for non-cutting shaping

Abstract: The invention relates to lubricants containing one or more paraffin-free mineral oil raffinate(s) and one or more organic phosphorus compound(s) and/or sulphur compound(s) and/or optionally amine(s) and/or optionally adhesion promoter(s), which, in addition to the paraffin-free mineral oil raffinate(s), contain the following constituents: a) from 0.01 to 3.0 % by weight of polyethylene glycol monoethers and/or polyethylene glycol monoesters of the formula in which R1 and n are as defined in claim 1, b) from 0.5 to 10.0 % by weight of aliphatic alcohols and/or esters of aliphatic alcohols with alkane carboxylic acids, c) from 0.1 to 10.0 % by weight of alkanolamine esters and/or alkanolamine ester salts of the general formula(e) in which x, R3, R4 and R5 are as defined in claim 1, and optionally d) from 0.1 to 2.0 % by weight of dicycloalkylamines, dialkylamines and/or N-(alkyl)-N-(phenyl) amines and/or their salts and/or esters and/or ester salts of trialkanolamines with carboxylic acids as corrosion inhibitor(s).

Operation of continuous extraction process

Abstract: Method of operation for a continuous countercurrent extraction zone, to which a charge mixture stream and a solvent stream are continuously supplied and from which an extract stream and a raffinate stream are continuously withdrawn. In one embodiment, the method comprises establishing a recycle stream consisting of a portion of the light phase stream withdrawn from the column, combining the recycle stream with the charge mixture stream, and controlling the streams flowing to and from the column. The combined feed stream to the extraction zone is controlled at a constant flow rate and recycle flow has preference over charge mixture flow, thereby causing charge stream flow to vary inversely with recycle flow. An important feature of the invention resides in adjustment of composition of this total combined feed stream to the extraction zone in order to deal with fluctuations in other parameters. The effects of fluctuations in flow rates and compositions of streams entering and leaving an extraction zone are mitigated, resulting in increased efficiency.

Improved removal of phenols from water

Abstract: In a process for purification of wastewater streams containing phenolic impurities wherein the wastewater stream is contacted with an ether extraction solvent for the extractive removal of the phenolic impurities, to form an ether extract phase containing at least a portion of the phenolic impurities and an aqueous raffinate phase depleted in the phenolic impurities, the improvement which comprises effecting the separation of the phases in the presence of a phase separation promoting amount of at least one polyhydric alcohol

Process for the deoiling of olefin sulphonates

Abstract: An improved process for the solvent extraction of free oil from C 8 to C 24 olefin sulfonation products, which comprises steps for contacting an olefin sulfonation product containing free oil with an alkane-based extraction solvent and phase separating the resulting mixture into an extract phase enriched in free oil and a raffinate phase enriched in sulfonated matter. The invention is particularly directed to the use in such a process of an extraction solvent which comprises one or more C 4 to C 9 alkanes and between about 5 and 35 percent by weight of dimethyl ketone. Deoiled sulfonation products are known for utility as components of detergent formulations for industrial, household and personal care uses.

Preparation of sugar solution containing little oligosaccharide

Abstract: PURPOSE:To prepare a sugar solution, containing little oligosaccharide, and reincorporable into a saccharified starch solution, by reacting alpha-glucosidase with a diluted hydrol solution or raffinate. CONSTITUTION:alpha-Glucosidase derived from a microorganism or plant is reacted with a solution obtained by diluting hydrol formed as a by-product in producing crystal glucose or raffinate formed as a by-product in producing high-fructose isomerized sugar solutions from isomerized sugar solutions at 50-60 deg.C for 1- 24hr.

Process for working up vanadium-containing used catalysts

Abstract: The process provides: leaching of the vanadium-containing used catalyst in the presence of vanadium(II) ions; separation of the slurry obtained into a solid support which after the treatment is used for the preparation of the vanadium catalyst, and into a solution, a portion of which is passed to electrochemical treatment which is carried out with a cathodic current density of from 100 to 300 A/m to obtain the vanadium(II) solution, and recycling said solution to the leaching stage; oxidation of vanadium(IV) to vanadium(V); extraction of vanadium(V) with aliphatic amines, treated with sulphuric acid; reextraction of vanadium(V) in the presence of ammonium persulphate; passing the sulphuric acid through the layer of the solid ammonium vanadate obtained at a weight ratio of 1:2 to 3 to produce vanadium pentoxide; evaporation to dryness and crystallization of the raffinate obtained after the extraction to produce potassium alum; evaporation to dryness and crystallisation of the solution produced after ammonium vanadate has been isolated therefrom, to obtain ammonium sulphate.

Improved alcohol recovery process

Abstract: of EP0175443According to the process of the present invention, alcohols are recovered from aqueous mixtures thereof with a concentrated strong acid by contacting such alcohol-containing aqueous concentrated acid mixtures with a carboxylic acid selected from the group consisting of acids of the formula RCO2H wherein R is a straight or branched-chain or cyclic alkyl of from 5 to 19 carbon atoms per molecule to form an extract phase containing the carboxylic acid in addition to said alcohol, and an aqueous raffinate phase depleted in the alcohol.