Showing papers on "Raffinate published in 1989"

Purification of hydrocarbonaceous fractions

Abstract: A process for recovering diamondoid compounds from hydrocarbonaceous minerals and/or from deposits left by such minerals in equipment or otherwise, which comprises dissolving diamondoid compounds in an aromatic distillate fuel oil; extracting aromatics from the solution; and separating diamondoid compounds from the raffinate of the extraction.

Simulated moving bed chromatographic separation

Abstract: A method and apparatus for separation of an extract component from a raffinate component in a simulated moving bed chromatographic separation train system. The system includes a plurality of beds, packed with a sorbent material, connected to form a closed recycle loop. Inlets to the train are provided for a feed stream and a desorbent stream along with outlets for removal of a raffinate stream and an extract stream. Increased product throughput and yield are obtained by intermittantly introducing and withdrawing the various streams to the train while continuously recycling a portion of the fluid in the system.

Method for recovering and using lignin in adhesive resins by extracting demethylated lignin

Abstract: Lignin, or a lignin derived material, which has been significantly demethylated (eg, the demethylated lignin found in the raffinate produced as a by-product of dimethyl sulfide production which can be carried out using the spent liquor from wood pulping operations) can be isolated by a process wherein an organic solvent is added to a lignin-containing aqueous solution The organic solvent is typically a polar, and at least a partially water-immiscible substance such as, for example, ethyl acetate The resulting lignin-containing aqueous solution/organic solvent mixture is acidified to produce a water layer which is discarded and an organic solvent layer which contains the demethylated lignin Upon its recovery, the demethylated lignin is dissolved in an alkaline solution to which an aldehyde source is added to produce a resol-type resin The aldehyde source may be formaldehyde in solution, paraformaldehyde, hexamethylenetetramine, or other aldehydes including acetaldehyde, furfural, and their derivatives

Extraction of crude methanol and conversion of raffinate

Abstract: An improved process for reacting crude aqueous methanol feedstock with tertiary-olefinic hydrocarbons to produce C5+ methyl tertiary-alkyl ethers, which comprises: contacting the aqueous methanol feedstock with a liquid hydrocarbon extractant rich in C4+ isoalkene under liquid extraction conditions; recovering an organic extract phase comprising the hydrocarbon extractant and a major amount of methanol introduced in the feedstock; reacting the extracted methanol and C4+ isoalkene in contact with an acid etherification catalyst under catalytic reaction conditions to produce ether product; separating ether product from unreacted methanol and olefin; recovering an aqueous methanol raffinate phase containing the major amount of water introduced with the feedstock and a minor amount of feedstock methanol; and converting methanol from the aqueous raffinate phase concurrently with unreacted methanol and olefin from etherification effluent separation to produce hydrocarbons.

Process for recovering metal values such as scandium, iron and manganese from an industrial waste sludge

Abstract: A process for eliminating an industrial waste sludge by converting its metal values into useful products involves the selective leaching of Mn, divalent Fe, and other valuable metals, such as Sc, Co, Cr, Ni, Th, rare earths, etc. with a mixture of dilute sulfuric acid and a reductant at ambient temperature. Scandium is recovered by passing the leachate through an ion exchange column which is packed with a weakly cationic resin. The retention of other metals on the resin column is negligible. The scandium is eluted from the resin column and converted to a solid product. The raffinate from the ion exchange column is titrated with an alkali solution to convert the metals, except divalent Mn and Fe, to a solid metal hydroxide. After the separation the filtrate is treated with an alkali and an oxidant to recover iron as a solid product of iron oxide which is separated from the solution. The remaining solution contains only Mn values which are recovered by treating the solution with an alkali and an oxidant to yield a solid manganese product. Separation of the solid leaves a liquid that can be discharged directly. The residue from the initial acid leaching contains the remaining metal values. HCl is used to selectively dissolve the Fe values. The insoluble residue is digested in an alkali to extract the total tungsten values. The residue from the alkali digestion contains substantial amounts of Ta, Nb and Ti and is a viable source for these metals.

Production of ether-rich fuel

Abstract: Methanol or other alcohol is converted to high octane gasoline components by an integrated process wherein crude aqueous alcohol feedstock is extracted with a liquid extractant stream containing C 4 + iso-olefin and reacted to form tertiary-alkyl ethers, such as MTBE. The aqueous raffinate is converted to predominantly gasoline range liquid hydrocarbons in a MTG catalytic reactor, with byproduct alkanes rich in propane and isobutane. Dehydrogenation of C 3 -C 5 alkanes from the MTG unit provides propene and isobutene reactants for subsequent etherification steps. Propene from the MTG dehydrogenation step is reacted with water to produce di-isopropyl ether, which may be blended with MTBE and C 6 + MTG hydrocarbons to produce high octane gasoline. Isobutylene and isoamylenes from the MTG dehydrogenation step can be removed and recycled as a liquid extractant stream.

Two-step heterocyclic nitrogen extraction from petroleum oils

Abstract: A process for the removal of basic heterocyclic nitrogen compounds from petroleum oils which comprises: (a) contacting said petroleum oils containing basic heterocyclic nitrogen compounds with an aqueous solution of an acidic solvent at extraction conditions in a first contacting zone, (b) separating the product of step (a) into a raffinate product stream comprising hydrocarbons having a lean content of basic heterocyclic nitrogen compounds and residual acid levels, and a first extract phase comprising hydrocarbons, water and acid having a substantial content of basic heterocyclic nitrogen compounds, (c) contacting said first extract phase with a hydrocarbon solvent which is substantially immiscible with said first extract phase at extraction conditions in a second contacting zone, and (e) separating the product of step (c) into a hydrocarbon recovery stream comprising the immiscible hydrocarbon solvent and oil-derived hydrocarbons having a lean content of basic heterocyclic nitrogen compounds and a second extract phase comprising acid, water and a decreased amount of nitrogen-free hydrocarbons and having a high content of basic heterocyclic nitrogen compounds.

Integrated process for production of gasoline and ether from alcohol with feedstock extraction

Abstract: Alcohol feedstock containing water is extracted with olefinic liquid and reacted catalytically to produce tertiary ether. Unreacted alcohol and olefin vapor separated from etherification effluent is converted along with aqueous alcoholic raffinate in a zeolite catalysis step to produce gasoline and paraffinic intermediate. By dehydrogating the C3 -C5 paraffins, an olefinic liquid rich in isoalkenes is obtained for recycle to the extractor as solvent for alcohol feedstock.

Etherification of extracted crude methanol and conversion of raffinate

Abstract: An improved process for reacting crude aqueous methanol feedstock with iso-olefinic hydrocarbons to produce C5+ methyl tertiary-alkyl ethers, which comprises: contacting the aqueous methanol feedstock with a liquid hydrocarbon extractant rich in C4+ iso-alkene under liquid extraction conditions; recovering an organic extract phase comprising the hydrocarbon extractant and a major amount of methanol introduced in the feedstock; reacting the extracted methanol and C4+ isoalkene in contact with an acid etherification catalyst under catalytic reaction conditions to produce ether product; recovering an aqueous methanol raffinate phase containing the major amount of water introduced with the feedstock and a minor amount of feedstock methanol; and converting methanol from the aqueous raffinate phase to produce hydrocarbons.

Method for processing heavy crude oils

Abstract: A method for processing heavy crude oils comprising a) atmospheric distillation of a heavy crude oil having a high content of metals, asphaltenes and sulfur; b) solvent extraction of the atmospheric distillation residue to obtain an extract with characteristics equivalent to those which an atmospheric residue derived from light crude oil and a raffinate fraction, solid at ambient conditions, in which are concentrated the asphaltenes, metals and sulfur present in the original crude oil; c) vacuum distillation of the deasphalted extract, obtaining a light fraction or gas oils with characteristics adequate to be subjected to a secondary conversion process, plus a bottoms fraction or vacuum residue; d) treatment of the vacuum gas oils in a conversion stage and e) subjecting the bottoms of raffinate from the extraction stage to a metallurgical process, in admixture with cokeable coal and coke fines to production of metallurgical coke.

Chromatographic separation process for recovering individual diethyltoluene isomers

Abstract: A process for separating 3,5-diethyltoluene (3,5-DET) and/or 2,6-diethyltoluene (2,6-DET) from a feed mixture comprising at least one isomer from the group 3,5- and 2,6-diethyltoluene and at least one other isomer thereof, which process comprises contacting the mixture at adsorption conditions with an adsorbent comprising an X zeolite, cation exchanged with a mixture of barium and potassium or sodium, lithium, barium or copper cations or mixtures thereof or a Y zeolite cation exchanged with barium, calcium, sodium, potassium or copper cations or mixtures thereof, thereby selectively adsorbing one or more of said isomers and removing one or more relatively non-adsorbed isomer(s) from contact with the adsorbent. 2,6-diethyltoluene is the most strongly adsorbed isomer with certain adsorbents and is recovered by desorption at desorption conditions with a desorbent material comprising a monocyclic alkyl-substituted aromatic hydrocarbon, e.g., p-diethylbenzene, m-diethylbenzene, p-xylene or p-toluene and optionally, a diluent, e.g., a straight chain or branched paraffin, e.g., n-heptane or iso-octane, an ether or a halogenated hydrocarbon. With certain adsorbents 3,5-DET is the least strongly adsorbed isomer and can be recovered in the raffinate. Certain of the adsorbent-cation combinations perform the dual function of strongly adsorbing 2,6-DET and least strongly adsorbing 3,5-DET.

Treatment and disposal options for a heavy metals waste containing soluble Technetium-99

Abstract: Various equipment decontamination and uranium recovery operations at the Portsmouth Gaseous Diffusion Plant generate a so-called ''raffinate'' waste stream characterized by toxic heavy metals, high concentrations of nitric aced, and low levels of radioactive nuclides (/sup 235/U and /sup 99/Tc). Dilution and adjustment of solution pH to a value of 8.2 to 8.5 precipitates the heavy metals that can be hydrolyzed, which are concentrated by paper filtration to yield a filter cake designed as heavy metals sludge (HMS) and HMS filtrate. The HMS fraction may be incorporated into cement-based grout containing ground blast furnace slag to dramatically reduce the mobility of its toxic and radioactive components. Sorption of soluble mercury, pertechnetate, and nitrate anions from the HMS filtrate was tested using organic resins and inorganic sorbents. Removal of Hg and /sup 99/Tc by ironing filings is efficient and economical, generating a small volume of spent sorbent amenable to co-disposal with HMS in a grout waste form. When a more rapid sorption is required, poly-4- vinylpyridine resin is very effective for the removal of soluble /sup 99/Tc, with little uptake of interfering anions at near-neutral influent pH values. 37 refs., 8 figs., 6 tabs.

Zirconium-hafnium separation process

Abstract: A process for separating zirconium values from hafnium values wherein an aqueous solution of ZrCl 4 and HfCl 4 is contacted with NH 4 SCN, feeding the resultant solution into a solvent extraction system containing aqueous HCl and MIBK, separating off the solvent phase containing MIBK, HSCN, hafnium thiocyanate complex, and any decomposition products of HSCN to leave the aqueous phase raffinate containing NH 4 Cl, zirconium oxide-chloride and low concentrations of HSCN, scrubbing the hafnium values from the separated solvent phase, treating the scrubbed solvent phase containing MIBK and HSCN with NH 4 OH to convert the HSCN to NH 4 SCN, separating the NH 4 SCN from the treated solvent phase, treating the separated solvent phase to remove essentially all thiazolines, and scrubbing residual HSCN from the raffinate with the desulfurized solvent phase.

Integrated system for extraction of crude alcohol and co-conversion raffinate with olefin

Abstract: An improved reactor system reacts crude aqueous methanol feedstock with iso-olefinic hydrocarbons to produce C 5 + methyl t-alkyl ethers. The system includes an extractor for contacting the aqueous methanol feedstock with a liquid hydrocarbon extraction solvent rich in C 4 + isoalkene. Both an organic extract phase and an aqueous methanol raffinate phase recovered from the extractor and fed to a primary reactor. This primary reactors reacts the methanol and C 4 + isoalkene from the organic extract phase under catalytic conditions to produce an ether product. The ether product is fed to an etherification effluent fractionator to separate the ether product from unreacted methanol and C 4 + isoalkene. A secondary reactor then converts methanol from the aqueous methanol raffinate phase with the unreacted methanol and C 4 + isolakene to produce hydrocarbons.

Method for the production of an aromate concentrate suitable for use as blending component for fuel

Abstract: In the method for the production of an aromate concentrate suitable for use as blending component for gasifier fuel, feed hydrocarbon mixtures having boiling ranges substantially between 40° and 170° C., are subjected, without any previous separation into individual fractions, to an extractive distillation employing N-substituted morpholine, substituents of which display no more than seven C-atoms, as selective solvent. Herewith, the lower boiling non-aromates with a boiling range up to about 105° C., practically completely, and most of the higher boiling non-aromates with a boiling range between about 105° and 160° C., are recovered as raffinate, whereas the aromates, which are to be employed in whole or in part as blending component, come down in the extract of the extractive distillation. In order to separate heavy aromates from solvent, a partial stream of the circulating solvent is mixed with water, and the heavy aromates are separated as a light phase from the solvent-water mixture. The solvent-water mixture is then separated into its components, which are re-utilized.

Process for separating glucose and mannose with dealuminated Y zeolites

Abstract: Glucose is separated from mixtures with mannose and other saccharides by adsorption on low aluminum Y-type zeolites, i.e., having up to about 50 atoms of aluminum per unit cell and desorbing the adsorbate with water. Glucose is removed from the adsorption process in the raffinate.

Adsorptive separation of para-xylene.

Abstract: Para-xylene is separated from other C₈ isomers and/or C₉ aromatics by contacting the para-xylene-containing feed mixture with an X or Y zeolite adsorbent having Group IA or IIA cations, e.g., barium and/or potassium at exchangeable cationic sites. The para-xylene is selectively adsorbed onto the adsorbent. The feed is then removed from the adsorbent and the para-xylene recovered from the resulting rich adsorbent by desorption with diethyltoluene. The C₉'s and the other xylene isomers are typically recovered in the desorbent-containing raffinate and can be separated from this desorbent by fractionation of the raffinate and the desorbent recycled to the process.

The System Acetone — Water — Glycerol and its Application in Liquid-Liquid Extraction of Proteins

Abstract: Acetone and glycerol are only partially miscible at room temperature. Addition of up to 50 mole-% water is allowed without removing the miscibility gap. By varying the water content, the polarities of the raffinate and extract phases can be adjusted to favorite conditions for the extraction of proteins. Thus, the system can be handled in common extraction columns, which is an important process design aspect. Recovery of proteins from both phases is very simple, as this liquid-liquid extraction system does not contain polymers of a molecular weight similar to the proteins. Distribution equilibria of peroxidase, alk, phosphatase and oxytocin will be given

Heat integration process

Abstract: A portion of the heat of vaporization, required to separate and recover methanol from wash water used to remove methanol from a C₄ raffinate resulting from the reaction of isobutene containing C₄ hydrocarbons and methanol to produce MTBE is recovered by conducting the distillation of the methanol/water mixture at a pressure of 40 to 60 psig, thereby increasing the temperature of the methanol overhead to 104 to 114° C and using the reaction effluent from the MTBE reactor to cool and condense the methanol overhead, said reactor effluent being correspondingly heated prior to entry into a debutanizer tower where unreacted C₄'s and methanol are removed as a raffinate and MTBE product recovered. It is this raffinate that is washed with water to recover the unreacted methanol, with the methanol/water mixture being distilled as set forth above. In another embodiment a stream having a lower temperature than the methanol overhead is withdrawn from the debutanizer and used to cool the methanol overhead, then the correspondingly heated stream returned to the debutanizer.

Removal of thorium from raffinate

Abstract: Thorium is removed from raffinate effluent by pre-washing with odorless kerosene to remove organic contaminants, followed by solvent extraction counter-currently with tri-n-octylphosphine oxide in odorless kerosene. The loaded solvent from the solvent extraction is back-washed with K 2 CO 3 solution at about 60° C., and subsequent lime addition precipitates Th(OH) 4 .

Uranium separation from high iron concentration by the use of ammonium pyrrolidine dithiocarbamate

Abstract: The method of uranium separation from high iron concentration by the use of ammonium pyrrolidine dithiocarbamate is described. The determination of Fe and U in raffinate solution was performed by radioisotope X-ray emission spectroscopy.

Extraction and reactor system

Abstract: An improved extraction and reactor system for reacting crude aqueous alcohol feedstock with iso-olefinic hydrocarbons to produce tertiary-alkyl ethers. This system is useful in extracting crude methanol in MTBE production. A typical feedstock separation and etherification reactor system for converting crude methanol feedstock to methyl tert-alkyl ether comprises: extractor means for contacting crude feedstock liquid with a liquid olefinic hydrocarbon extraction solvent to provide a liquid extract stream rich in methanol and an aqueous raffinate stream; first catalytic reactor means operatively connected for contacting the extract stream with etherification catalyst methanol to produce second catalytic reactor means, such as an FCC unit, for contacting the raffinate with methanol conversion catalyst in the presence of hydrocarbon to produce liquid olefinic hydrocarbon; and means for charging at least a portion of the liquid olefinic hydrocarbon product from the second reactor means to the extractor means as extraction solvent.

Zeolitic para-ethyltoluene separation with tetralin heavy desorbent

Abstract: A chromatographic process able to separate para-ethyltoluene from feed mixtures of C 8 and/or C 9 aromatic hydrocarbons. In the process, the para-ethyltoluene-containing feed mixture is contacted with a Y zeolite adsorbent having potassium at exchangeable cationic sites. The para-ethyltoluene is selectively adsorbed onto the adsorbent. The non-adsorbed components of the feed are then removed from the adsorbent and the para-ethyltoluene recovered by desorption with tetralin or alkyl or dialkyl derivatives of tetralin or alkyl derivatives of naphthalene. The other C 9 's and the xylene isomers in the raffinate and p-ethyltoluene in the extract can be separated from the heavy desorbent by fractionation of the raffinate or extract and the desorbent recycled to the process.

Alternatives for disposal of raffinate from the TRUEX process

Abstract: Possible methods for disposing of the immobilized raffinate from TRUEX processing are reviewed. The purpose of the TRUEX process is to extract transuranium elements from high-level and TRU wastes into a small volume that can be managed at lower cost than that of the original wastes. The raffinate from the TRUEX process, containing negligible concentrations of transuranium elements, would be combined with salt solutions also derived from processing high-level waste, and the mixture would be converted to grout.

Chiral epoxyalcohol recovery in asymmetric epoxidation process

Abstract: of EP0308188In the production of a chiral glycidol by reaction of an allylic alcohol and an organic hydroperoxide in an organic solvent in the presence of a metal catalyst, the chiral glycidol is effectively recovered by aqueous extraction of the reaction raffinate. This improves process economics by shortening process time and eliminating the use of expensive chemicals for unreacted hydroperoxide removal.

Process for the preparation of an aromatic concentrate useful as a blending component for carburetion fuels

Abstract: In the process for producing an aromatics concentrate suitable as a blending component for carburettor fuels, feed hydrocarbon mixtures of a boiling range essentially between 40 and 170 DEG C are subjected to an extractive distillation, without prior separation into individual fractions, the selective solvent used being N-substituted morpholines with substituents having not more than 7 C atoms. In this process, the low-boiling non-aromatics of a boiling range up to about 105 DEG C are virtually completely, and the higher-boiling non-aromatics of a boiling range between about 105 and 160 DEG C predominantly, obtained as the raffinate, while the aromatics which are used wholly or partly as a blending component arise in the extract from the extractive distillation. For the purpose of separating heavy aromatics off from the solvent, water is added in this process to a part stream of the circulated solvent and the heavy aromatics are separated as the light phase from the solvent/water mixture. The latter is then separated into its constituents and re-used.