Abstract: The present invention relates to a mesoporous polymeric separation material comprising one or more functional groups bound to metal ions from Cu, Zn, Ag, or Pd. Methods of producing the material, as well as methods for its preparation, and use of said material in separation of pesticides from food or feed products is disclosed.

Abstract: Purge fluid from a vessel head in an adsorption process is distributed to recovery processes according to the purity of product contained in the fluid. Extract-rich fluid thus is routed directly to recovery of the extract product. Distribution preferably is determined by internal positioning of feed, desorbent and product streams in the adsorption vessel.

Abstract: A process for separating a product from a multicomponent feedstream to an adsorption apparatus or system is described. The apparatus or system may comprise a moving-bed or a simulated moving-bed adsorption means. The product comprises at least one organic compound, such as an aryl compound with alkyl substitutes. In embodiments the conduits used to supply the feedstream to the apparatus or system are flushed with media of multiple grades. The improvement is a more efficient use of the desorbent. In embodiments the process achieves improvements in one or more of efficiency of adsorption separation, capacity of adsorption apparatus systems, and purity of product attainable by adsorption process.

Abstract: A process for the production of para-xylene by simulated counter-current adsorption with high flexibility with respect to a reference run (100%) uses 2 adsorbers each with 12 beds, said adsorbers being able to be connected in accordance with 3 different modes; the flexibility obtained is 50% to 150%.

Abstract: Adsorbents and methods for the adsorptive separation of para-xylene from a mixture containing at least one other C8 aromatic hydrocarbon (e.g., a mixture of ortho-xylene, meta-xylene, para-xylene, and ethylbenzene) are described. Suitable adsorbents comprise zeolite X having an average crystallite size of less than 1.8 microns. The adsorbents provide improved mass transfer, which is especially advantageous for improving productivity in low temperature, low cycle time adsorptive separation operations in a simulated moving bed mode.

Abstract: A process to reduce flush circulation rates in an adsorption separation system is presented. The flush stream is used to improve the capacity of the simulated moving bed system by flushing the contents of the transfer lines containing raffinate material back into the adsorbent column. The flush stream is a material that is used to flush the head chambers in the column, or from the rotary valve flush dome sealant.

Abstract: A process for separating a product from a multicomponent feedstream to an adsorption apparatus or system is described. The apparatus or system may comprise a moving-bed or a simulated moving-bed adsorption means. The product comprises at least one organic compound, such as an aryl compound with alkyl substitutes. In embodiments the conduits used to supply the feedstream to the apparatus or system are flushed with media of multiple grades. The improvement is a more efficient use of the desorbent. In embodiments the process achieves improvements in one or more of efficiency of adsorption separation, capacity of adsorption apparatus systems, and purity of product attainable by adsorption process.

Abstract: A process for separating a product from a multicomponent feedstream to an adsorption apparatus or system is described. The apparatus or system may comprise a moving-bed or a simulated moving-bed adsorption means. The product comprises at least one organic compound, such as an aryl compound with alkyl substitutes. In embodiments the conduits used to supply the feedstream to the apparatus or system are flushed with media of multiple grades. The improvement is more efficient use of the desorbent. In embodiments the process achieves improvements in one or more of efficiency of adsorption separation, capacity of adsorption apparatus systems, and purity of product attainable by adsorption process.

Abstract: The present invention relates to a process for recovering polar hydrocarbons from non-polar hydrocarbons, such as aromatics from non-aromatics, naphthenes from paraffins and isoparaffins, or olefins from paraffins and isoparaffins, in feed mixtures containing at least a measurable amount of heavier hydrocarbons. According to the invention, an improved extractive distillation (extractive-distillation) process is disclosed for recovering aromatic hydrocarbons including benzene, toluene, and xylenes from heavy (C9+) hydrocarbons. The invention also relates to an improved extractive-distillation process for recovering mainly benzene and toluene from the C6-C7 petroleum streams containing at least a measurable amount of C8+ hydrocarbons.

Abstract: The present process comprises a means for energy savings in one or more process pumps by driving the one or more pumps with a variable-speed driving means. The invention is particularly useful in the separation of an adsorbed product from a mixture of components using simulated-moving-bed adsorption associated with a large circulating stream pumped with variable-speed driving means for conservation of energy relative to the known art. The improvement is particularly applicable to a process for the separation of para-xylene from mixed C8 aromatics.

Abstract: The present invention is related with the application of an adsorbent material of microporous carbon (MCA), prepared from the direct pyrolysis of copolymers generically known as Saran, in adsorption processes to reduce the benzene content in naphtha boiling range hydrocarbon streams, between 27 and 191° C., in which is preferable to perform a first separation by distillation of the C6's fraction, and a further separation of Benzene by adsorption through an adsorbent material bed, obtaining the fraction of C6's free of Benzene and an adsorbent with Benzene, which is further regenerated by pressure or temperature swing desorption or by displacement using a desorbent such as an inert gas at high temperature or by passing a desorbent which after the process, the desorbent and Benzene are separated by distillation. The fraction of C6's free of Benzene is reintegrated to the hydrocarbon stream and providing a gasoline with a Benzene content less than 1 volume %.

Abstract: A process is presented for the selective separation and recovery of large normal paraffins from a heavy kerosene boiling point fraction. The process includes passing the heavy kerosene fraction through an adsorption separation system for separating the normal paraffins from the paraffin mixture. The recovered extract and raffinate streams are mixed with a diluent made up of a lighter hydrocarbon. The subsequent diluted extract and raffinate streams are passed through first fractionation columns to separate the desorbent from the diluent and the heavier paraffins. The mixture of the diluent and heavier paraffins is passed through a second set of fractionation columns to separate the diluent and the heavier paraffins.

Abstract: The invention relates to an improved absorption-type separation and/or purification processes having dual rotary valves.

Abstract: The invention relates to processes for reducing the sulfur content in hydrocarbon fuels such as gasoline, diesel fuel and jet fuel. The invention provides a method and materials for producing ultra low sulfur content transportation fuels for motor vehicles as well as for applications such as fuel cells. The materials and method of the invention may be used at ambient or elevated temperatures and at ambient or elevated pressures without the need for hydrogen.

Abstract: A process for producing an adsorbent where a metal oxide is reacted with an alkoxy silane to produce an epoxy-functionalized metal oxide. This product is reacted with an amino-substituted propionic acid and a nitro-substituted fluorenone, and this product is grafted to the epoxy-functionalized metal oxide. This grafted product is the adsorbent, which may be contacted with a hydrocarbon mixture having at least one sulfur containing compound in order to remove this sulfur containing compound. Also disclosed is a process for adding polymerization groups to an adsorbent.

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 Li/i+1 directly joining two successive plates Pi, Pi+, 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 Li/i+1 is adjusted so as to obtain the best performance of the SMB.

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.

Abstract: An exemplary embodiment can be a process for removing one or more polynuclear aromatics from at least one reformate stream from a reforming zone. The PNAs may be removed using an adsorption zone. The adsorption zone can include first and second vessels each vessel containing an activated carbon adsorbent. Generally, the process includes passing the at least a portion of an effluent of the reforming zone through the first vessel containing a first activated carbon adsorbent wherein the first activated carbon adsorbent comprises iron.

Abstract: A process is presented for the selective separation and recovery of large normal paraffins from a heavy kerosene boiling point fraction. The process includes passing the heavy kerosene fraction through an adsorption separation system for separating the normal paraffins from the paraffin mixture. The recovered extract and raffinate streams are mixed with a diluent made up of a lighter hydrocarbon. The subsequent diluted extract and raffinate streams are passed through first fractionation columns to separate the desorbent from the diluent and the heavier paraffins. The mixture of the diluent and heavier paraffins is passed through a second set of fractionation columns to separate the diluent and the heavier paraffins.

Abstract: Aromatic by-products are sorbed from mono-olefin-containing feedstocks of olefins having from about 6 to 22 carbon atoms per molecule that contain aromatic by-products having from 7 to 22 carbon atoms per molecule. A benzene-containing regenerant displaces and desorbs the aromatic by-products from the sorbent and a regeneration effluent is provided. The regeneration effluent is treated in a regeneration effluent distillation system to provide a benzene-rich stream and an aromatic by-products-containing stream. The latter is subjected to benzene-forming conditions and recycled to the regeneration effluent distillation system where benzene is recovered.

Abstract: Process for separation of metaxylene, with at least 99% by weight of purity of an aromatic feedstock F, in a single adsorption stage in a simulated moving bed in an SMB device that comprises 12, 13 or 15 adsorbent beds with different numbers of beds being employed in zone 1 between the supply of the desorbent D and the draw-off of the extract E; zone 2 between the draw-off of the extract E and the supply of the feedstock F; zone 3 between the supply of the feedstock and the draw-off of the raffinate R; and zone 4 between the draw-off of the raffinate R and the supply of the desorbent D whereby the process is carried out according to a configuration of zones (a, b, c, d), whereby a, b, c, and d represent the number of adsorbent beds that operate respectively in zones 1, 2, 3, 4 in which there is used: Either an SMB of 12 adsorbent beds operating according to the configuration (2, 5, 3, 2), Or an SMB of 13 adsorbent beds operating according to the configuration (2, 5, 4, 2), Or an SMB of 15 adsorbent beds op

Abstract: Adsorbents and methods for the adsorptive separation of para-xylene from a mixture containing at least one other C8 aromatic hydrocarbon (e.g., a mixture of ortho-xylene, meta-xylene, para-xylene, and ethylbenzene) are described. Suitable binderless adsorbents (e.g., formulated with the substantial absence of an amorphous material that normally reduces selective pore volume), particularly those with a water content from about 3% to about 5.5% by weight, improve capacity and/or mass transfer. These properties are especially advantageous for improving productivity in low temperature, low cycle time adsorptive separation operations in a simulated moving bed mode.

Abstract: Adsorbents and methods for the adsorptive separation of para-xylene from a mixture containing at least one other C8 aromatic hydrocarbon (e.g., a mixture of ortho-xylene, meta-xylene, para-xylene, and ethylbenzene) are described. Suitable adsorbents comprise small-crystallite-size zeolite X having an average crystallite size of less than 1.8 microns. The adsorbents may be binderless (e.g., formulated with the substantial absence of an amorphous material that normally reduces selective pore volume) to further improve capacity and mass transfer. These properties are especially advantageous for improving productivity in low temperature, low cycle time adsorptive separation operations in a simulated moving bed mode.

Abstract: This invention relates to a process for conversion of hydrocarbon feedstock, comprising the steps of (A) feeding the hydrocarbon feedstock to an adsorption unit; (B) adsorbing the hydrocarbon feedstock in the adsorption unit with a solid particulate adsorbent useful for adsorbing at least one component from the hydrocarbon feedstock under adsorption conditions; (C) withdrawing the adsorbed feedstock from the adsorption unit; (D) desorbing the component(s) from the solid particulate adsorbent; and (E) removing, under the adsorption conditions for a fractional time of step (B), at least a portion of said adsorbent while the feedstock is being fed to the adsorption unit.

Abstract: Process for separating paraxylene with a purity that is at least equal to 99.5% by weight from an aromatic feedstock F in a single adsorption stage in a simulated moving bed (SMB), comprising different numbers of beds, allocated to a zone 1 between the supply of the desorbent D and the draw-off of the extract E; a zone 2 between the draw-off of the extract E and the supply of the feedstock F; a zone 3 between the supply of the feedstock and the draw-off of the raffinate R; a zone 4 between the draw-off of the raffinate R and the supply of the desorbent D, wherein an SMB of 12 adsorbent beds has bed configuration (2, 5, 3, 2), an SMB of 15 adsorbent beds has bed configuration (3, 6, 4 , 2), or an SMB of 19 adsorbent beds has bed configuration (4, 7, 6, 2), wherein the desorbent in this latter case is paradiethylbenzene.

Abstract: Aromatic by-products are sorbed from mono-olefin-containing feedstocks of olefins having from about 6 to 22 carbon atoms per molecule that contain aromatic by-products having from 7 to 22 carbon atoms per molecule. A benzene-containing regenerant displaces and desorbs the aromatic by-products from the sorbent and a regeneration effluent is provided. The regeneration effluent is treated in a regeneration effluent distillation system to provide a benzene-rich stream and an aromatic by-products-containing stream. The latter is subjected to benzene-forming conditions and recycled to the regeneration effluent distillation system where benzene is recovered.

Abstract: Adsorbents and methods for the adsorptive separation of meta-xylene from a mixture containing at least one other C8 aromatic hydrocarbon (e.g., a mixture of ortho-xylene, meta-xylene, para-xylene, and ethylbenzene) are described. Suitable adsorbents comprise sodium zeolite Y having an average crystallite size from about 50 to about 700 nanometers. The adsorbents provide improved separation efficiency, which may be associated with a higher meta-xylene mass transfer rate and/or other beneficial effects. Exemplary desorbents for use in the process may comprise toluene, benzene, or indan.

Abstract: The invention concerns a process for separating meta-xylene from a hydrocarbon feed comprising isomers containing 8 carbon atoms, comprising: a step for bringing said feed into contact with a faujasite type zeolite adsorbant, the percentage of water in the adsorbant being in the range 0 to 8% by weight and the adsorption temperature being from 25° C. to 250° C.; a desorption step employing a solvent selected from tetraline and its alkylated derivatives; a step for separating meta-xylene from the desorbant.

Abstract: In a process for producing a para-xylene enriched product from a gaseous mixture comprising at least para-xylene, meta-xylene and ortho-xylene, the gaseous mixture is contacted with an adsorbent capable of selectively adsorbing para-xylene and comprising a crystalline molecular sieve having an average crystal size between about 0.5 micron and about 20 microns. The contacting is conducted at a temperature and pressure such that at least part of the para-xylene in the mixture is adsorbed by the adsorbent to produce a para-xylene-depleted effluent stream. The para-xylene is then desorbed from said adsorbent and collected to form a para-xylene enriched stream. The adsorption and desorption steps are repeated for a plurality of cycles, such that the time between successive contacting steps is no more than 10 seconds.

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.

Abstract: Product purity from or capacity of a simulated-moving-bed adsorptive separation process is increased by flushing the contents of the transfer line previously used to remove the raffinate stream away from the adsorbent chamber, preferably into the raffinate column used to separate desorbent from raffinate product. Preferably a stream from the adsorbent chamber at an intermediate point between the feed entry point and raffinate withdrawal is used as the flushing liquid. This flush step eliminates the passage of a quantity of the raffinate material into the adsorbent chamber in the transfer-line flush period or when the process conduit is subsequently used to charge the feed stream to the adsorbent chamber.

Abstract: A process for separating mixtures of hydrocarbon isomers on molecular sieves, including providing columns which include molecular sieves and function alternatively as secondary adsorption, primary adsorption, and desorption devices, feeding the mixtures of hydrocarbon isomers to a column functioning as the primary adsorption device for adsorbing isomers with greater selectivity towards the molecular sieves, feeding effluent of the mixtures from the column functioning as the primary adsorption device to a column functioning as the secondary adsorption device for adsorbing remaining isomers with greater selectivity, discharging isomers with a lower selectivity from the column functioning as the secondary adsorption device and a desorbing agent therein, feeding a desorbing agent to the column functioning as the desorption device, discharging isomers with a greater selectivity towards the molecular sieves and the desorbing agent in the column functioning as the desorption device.

Abstract: The present invention relates to agglomerated zeolitic adsorbents based on zeolite X with an Si/Al ratio such that 1.15<Si/Al?1.5, at least 90% of the exchangeable cationic sites of the zeolite X of which are occupied either by barium ions alone or by barium ions and potassium ions whose Dubinin volume is greater than or equal to 0.240 cm3/g. They are obtained by agglomerating zeolite powder with a binder, followed by the zeolitization of the binder, the exchange of the ions of the zeolite by barium ions (and potassium ions) and the activation of the adsorbents thus exchanged. These adsorbents are particularly suited to the adsorption of the para-xylene present in C8 aromatic hydrocarbon fractions in the liquid phase in processes of simulated moving bed type but also to the separation of sugars, polyhydric alcohols, cresols or substituted toluene isomers.

Abstract: A process for separating multibranched paraffins comprised in a hydrocarbon feed comprising hydrocarbons containing 5 to 8 carbon atoms per molecule comprises a separation unit functioning by adsorption and contains at least one zeolitic adsorbent with a mixed structure with principal channels with openings defined by a ring containing 10 oxygen atoms and secondary channels with openings defined by a ring of at least 12 oxygen atoms, the secondary channels only being accessible to the feed to be separated via the principal channels. Particular zeolitic adsorbents of the invention are zeolites with structure types EUO, NES and MWW. NU-85 and NU-86 zeolites are also particularly suitable for carrying out the process of the invention.

Abstract: A method for concentrating 2,6-dimethylnaphthalene in a dimethylnaphthalene isomer mixture includes supplying the dimethylnaphthalene isomer mixture to an adsorption column packed with Y-type zeolite. In this instance, by setting the value derived from the expression (u1/3/&egr;)d−5/3 at 14 (m5/3 s−1/3 kg−1) or more, the concentration ratio of 2,6-dimethylnaphthalene to 2,7-dimethylnaphthalene can be 2.0 or more. u here represents the linear velocity (m/s) of the dimethylnaphthalene isomer mixture supplied to an adsorption column, &egr; represents the packing density (kg/m3) of Y-type zeolite, and d represents the grain size (m) of the Y-type zeolite.

Abstract: The performance of an adsorptive separation process recovering para-xylene from a C8 aromatic hydrocarbon feed mixture is improved by operating the process at higher desorbent purity. The improved performance allows for tradeoffs in other operating parameters and rates or improved product rates. The process preferably employs a barium and potassium exchanged zeolitic molecular sieve as the adsorbent and toluene as the desorbent.

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.

Abstract: A pressure swing adsorption process to separate para-xylene and ethylbenzene from a C8 aromatics stream produced by toluene conversion uses a para-selective adsorbent, preferably a non-acidic, medium pore molecular sieve of the MFI structure type, and is operated isothermally in the vapor phase at elevated temperatures and pressures. A fixed bed of adsorbent is saturated with pX and EB, which are preferentially adsorbed, then the feed to the process is stopped. Lowering the partial pressure desorbs the pX and EB giving a pX/EB-rich effluent. A stream of non-adsorbed mX and oX may be obtained before desorbing pX and EB.

Abstract: A pressure swing adsorption process to separate para-xylene and ethylbenzene from C8 aromatics uses a para-selective adsorbent, preferably a non-acidic, medium pore molecular sieve of the MFI structure type, and is operated isothermally in the vapor phase at elevated temperatures and pressures. A fixed bed of adsorbent is saturated with para-xylene and ethylbenzene, which are preferentially adsorbed, then the feed to the process is stopped. Lowering the partial pressure desorbs the para-xylene and ethylbenzene. The process effluent is rich in para-xylene and ethylbenzene. A stream of non-adsorbed meta-xylene and ortho-xylene may be obtained prior to desorption of para-xylene and ethylbenzene.

Abstract: CuY and AgY zeolites as selective sorbents for desulfurization of liquid fuels. Thiophene and benzene were used as the model system, and vapor phase isotherms were measured. Compared with NaY, CuY and AgY adsorbed significantly larger amounts of both thiophene and benzene at low pressures. It is hypothesized that this is due to &pgr;-complexation with Cu+ and Ag+. On a per-cation basis, more thiophene was adsorbed by Cu+ than by Ag+, eg. 0.92 molecule/Cu+ versus 0.42 molecule/Ag+ at 2×10−5 atm and 120° C. Molecular orbital calculations confirmed the relative strengths of &pgr;-complexation: thiophene>benzene and Cu+>Ag+. The experimental heats of adsorption for &pgr;-complexation are in qualitative agreement with theoretical predictions. The invention further comprises a process and sorbents for removal of aromatics from hydrocarbons.

Abstract: A coproduction process for ortho-xylene and para-xylene starting with a batch of hydrocarbons comprising two separation steps is described. The first step relates to a simulated counter-current fluidized bed system in a chromatographic column (6) containing at least five zones, comprising injection (1) of the batch and injection (2) of desorption agent and delivering an extract (3), a refined product (5), and an intermediate refined product (4). The extract is distilled (7) to obtain para-xylene (10) that is very pure or that can be purified by crystallization. The refined products are withdrawn continuously or discontinuously. Refined product (5), richer in ortho-xylene than the intermediate refined product, is distilled (9) to extract desorption agent (15) and is injected, according to the second step of the process, into a simulated counter-current fluidized bed system (17) delivering an extract (18) and a refined product (19) continuously.

Abstract: A pressure swing adsorption process to separate para-xylene and ethylbenzene from C8 aromatics which uses a para-selective, non-acidic, medium pore molecular sieve of the MFI structure type and is operated isothermally in the vapor phase at elevated temperatures and pressures is integrated with simulated moving bed adsorption (SiMBAC) to produce para-xylene product. A fixed bed of adsorbent is saturated with pX and EB, which are preferentially adsorbed, the feed is stopped, and lowering the partial pressure desorbs the pX and EB. The process effluent, which is rich in pX and EB, is subjected to SiMBAC to obtain para-xylene product.

Abstract: A pressure swing adsorption process to separate para-xylene and ethylbenzene from C8 aromatics which uses a para-selective, non-acidic, medium pore molecular sieve of the MFI structure type and is operated isothermally in the vapor phase at elevated temperatures and pressures is integrated with crystallization to produce para-xylene product. A fixed bed of adsorbent is saturated with pX and EB, which are preferentially adsorbed, the feed is stopped, and lowering the partial pressure desorbs the pX and EB. The process effluent, which is rich in pX and EB, is crystallized to obtain para-xylene product.

Abstract: The performance of an adsorptive separation process recovering para-xylene from a C8 aromatic hydrocarbon feed mixture is improved by operating the process at higher desorbent purity. The improved performance allows for tradeoffs in other operating parameters and rates or improved product rates. The process preferably employs a barium and potassium exchanged zeolitic molecular sieve as the adsorbent and toluene as the desorbent.

Abstract: A pressure swing adsorption process to separate para-xylene and ethylbenzene from C8 aromatics which uses a para-selective, non-acidic, medium pore molecular sieve of the MFI structure type and is operated isothermally in the vapor phase at elevated temperatures and pressures is integrated with simulated moving bed adsorption (SiMBAC) to produce para-xylene product. A fixed bed of adsorbent is saturated with pX and EB, which are preferentially adsorbed, the feed is stopped, and lowering the partial pressure desorbs the pX and EB. The process effluent, which is rich in pX and EB, is subjected to SiMBAC to obtain para-xylene product.

Abstract: A pressure swing adsorption process to separate para-xylene and ethylbenzene from a C8 aromatics stream produced by toluene conversion uses a para-selective adsorbent, preferably a non-acidic, medium pore molecular sieve of the MFI structure type, and is operated isothermally in the vapor phase at elevated temperatures and pressures. A fixed bed of adsorbent is saturated with pX and EB, which are preferentially adsorbed, then the feed to the process is stopped. Lowering the partial pressure desorbs the pX and EB giving a pX/EB-rich effluent. A stream of non-adsorbed mX and oX may be obtained before desorbing pX and EB.

Abstract: Construction and operational costs of recovering the extract or raffinate product of a simulated moving bed adsorptive separation process units are reduced by employing a dividing wall column to perform the separation. The raffinate or extract stream is passed into the column at an intermediate point on the first side of the dividing wall, with the column delivering the adsorptive separation product as a sidedraw from the opposite side of the dividing wall. A stream of co-adsorbed impurity is removed as an overhead stream and desorbent is recovered as a net bottoms stream.

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.

Abstract: The present invention relates to methods for removing VOCs from an aqueous polymer dispersion (e.g., an SBR latex) in which the dispersion is contacted with a stripping medium in the presence of a particulate adsorbent such as activated carbon. This process results in the rapid and economical removal of VOCs from polymer dispersions.

Abstract: A process for separating off cycloalkenes having at least two double bonds from a reaction mixture in hydrocarbon solution formed during the metathesis of cycloalkamonoenes or cyclomonoene/cyclopolyene mixtures comprising the steps of treating the reaction mixture with zeolites in the liquid phase, absorbing the olefins having at least two double bonds present in the solution by the zeolite, separating off the laden zeolite, and obtaining the cycloalkadienes and cyclopolyenes by desorption.