Abstract: One exemplary embodiment can be a process for regenerating catalyst in a fluid catalytic cracking unit. Generally, the process includes providing a feed to a riser of a reaction vessel, and providing a stream to a distributor positioned within a void proximate to an inlet receiving unregenerated catalyst in a regenerator.

Abstract: Processes for producing aromatics from a naphtha feedstream are provided. An exemplary process includes passing the feedstream to a fractionation unit, thereby generating a first stream including hydrocarbons having less than 8 carbon atoms and a second stream including hydrocarbons having at least 8 carbon atoms. The first stream is passed to a first reformer operated at a first set of reaction conditions to generate a first product stream. The first set of reaction conditions includes a first temperature and a first pressure. The second stream is passed to a second reformer operated at a second set of reaction conditions to generate a second product stream. The second set of reaction conditions includes a second temperature and a second pressure. The first pressure is lower than the second pressure.

Abstract: A method for controlling 2-isomer content in linear alkylbenzene obtained by alkylating benzene with olefins and catalyst used in the method.

Abstract: A process is presented for controlling the output of monoalkylated benzenes. The alkylbenzenes are linear alkylbenzenes and the process controls the 2-phenyl content of the product stream. The control of the process to generate a linear alkylbenzene with a 2-phenyl content within a desired range by recycling a portion of the effluent from the alkylation reactor to the inlet of the reactor.

Abstract: A new family of coherently grown composites of TUN and IMF zeotypes have been synthesized. These zeolites are represented by the empirical formula. NanMmk+TtAl1-xExSiyOz where “n” is the mole ratio of Na to (Al+E), M represents a metal or metals from zinc, Group 1, Group 2, Group 3 and or the lanthanide series of the periodic table, “m” is the mole ratio of M to (Al+E), “k” is the average charge of the metal or metals M, T is the organic structure directing agent or agents, and E is a framework element such as gallium. These zeolites are similar to TNU-9 and IM-5 but are characterized by unique compositions and synthesis procedures and have catalytic properties for carrying out various hydrocarbon conversion processes and separation properties for carrying out various separations.

Abstract: A new family of coherently grown composites of TUN and IMF zeotypes have been synthesized. These zeolites are represented by the empirical formula. NanMmk+TtAl1?xExSiyOz where “n” is the mole ratio of Na to (Al+E), M represents a metal or metals from zinc, Group 1, Group 2, Group 3 and or the lanthanide series of the periodic table, “m” is the mole ratio of M to (Al+E), “k” is the average charge of the metal or metals M, T is the organic structure directing agent or agents, and E is a framework element such as gallium. These zeolites are similar to TNU-9 and IM-5 but are characterized by unique compositions and synthesis procedures and have catalytic properties for carrying out various hydrocarbon conversion processes and separation properties for carrying out various separations.

Abstract: The xylene isomerization process unit and the transalkylation process units are combined in the present invention. A fractionation column can be shared by the two units, reducing the capital cost of the complex. In some embodiments, a split shell fractionation column and a split separator can be used.

Abstract: A new synthesis technique has been developed to prepare a family of coherently grown composites of at least two zeotypes. Examples of these composites are represented by the empirical formula. NanMmk+TtAl1-xExSiyOz where “n” is the mole ratio of Na to (Al+E), M represents at least one metal of zinc, Group 1, Group 2, Group 3 and the lanthanide series of the periodic table, and any combination thereof, “m” is the mole ratio of M to (Al+E), “k” is the average charge of the metal or metals M, T is the organic structure directing agent or agents, “t” is the mole ratio of N from the organic structure directing agent or agents to (Al+E), and E is a framework element such as gallium. The synthesis technique is the Layered Conversion Synthesis technique.

Abstract: A new family of coherently grown composites of TUN and IMF zeotypes have been synthesized. These zeolites are represented by the empirical formula. NanMmk+TtAl1-xExSiyOz where “n” is the mole ratio of Na to (Al+E), M represents a metal or metals from zinc, Group 1, Group 2, Group 3 and or the lanthanide series of the periodic table, “m” is the mole ratio of M to (Al+E), “k” is the average charge of the metal or metals M, T is the organic structure directing agent or agents, and E is a framework element such as gallium. These zeolites are similar to TNU-9 and IM-5 but are characterized by unique compositions and synthesis procedures and have catalytic properties for carrying out various hydrocarbon conversion processes and separation properties for carrying out various separations.

Abstract: A new family of coherently grown composites of TUN and IMF zeotypes has been synthesized and shown to be effective catalysts for aromatic transformation reactions. These zeolites are represented by the empirical formula. NanMmk+TtAl1-xExSiyOz where “n” is the mole ratio of Na to (Al+E), M represents at least one meta, “m” is the mole ratio of M to (Al+E), “k” is the average charge of the metal or metals M, T is the organic structure directing agent or agents, “t” is the mole ratio of N from the organic structure directing agent or agents to (Al+E), and E is a framework element such as gallium. The process involves contacting at least a first aromatic with the coherently grown composites of TUN and IMF zeotypes to produce at least a second aromatic.

Abstract: A reforming process includes an endpoint reduction zone for converting C11+ components via selective hydrogenation and hydrodealkylation to lower boiling point aromatics, such as benzene, toluene, and xylene, or their single ring aromatic C9-C10 precursors.

Abstract: A process according to various approaches includes flushing an intermediate transfer line at first flow rate during a first portion of the step-time interval. The process also includes flushing the intermediate transfer line at as second different flow rate during a second portion of the step-time interval so that a greater volume of fluid is flushed from the intermediate transfer line during one of the first portion and the second portion of the step-time interval than during the other of the first portion and the second portion of the step-time interval.

Abstract: Embodiments of simulated moving bed systems for separating a preferentially adsorbed component from a feed stream and processes for determining a pump-around profile of the simulated moving bed systems are provided. The process comprises the steps of rotating a rotary valve to a first valve position to direct the feed stream to a first adsorbent sub-bed. An intermediate stream between two adsorbent sub-beds in direct fluid communication with each other is irradiated with laser light that is directed from a probe of a Raman system positioned for inline sampling of the intermediate stream. Scattered light from the irradiated intermediate stream is collected with the probe. A spectrum of the scattered light is generated with the Raman system to determine concentrations of the preferentially adsorbed component and one or more other components in the intermediate stream.

Abstract: A process according to various approaches includes flushing residual fluid within an intermediate transfer line of a purification zone between a feed stream transfer line and the extract stream transfer line away from the adsorptive separation chamber to remove at least a portion of the residual fluid from the intermediate transfer line. The process may include directing the residual fluid flushed from the intermediate transfer line to another intermediate transfer line of the purification zone to flush residual fluid of the other transfer line into the purification zone for separation of the preferentially adsorbed component from the non-preferentially adsorbed component present in the other transfer line residual fluid.

Abstract: A process according to various approaches includes flushing an intermediate transfer line between the extract stream transfer line and the desorbent stream transfer line away from the adsorptive separation chamber to remove residual fluid from the intermediate transfer line. The process may include directing the residual fluid flushed from the intermediate transfer line to a downstream separation apparatus to separate components of the residual fluid.

Abstract: A process according to various approach includes flushing residual fluid within an intermediate transfer line of a purification zone defined as a region of the adsorptive separation chamber between the feed stream transfer line and the extract stream transfer line away from the adsorptive separation chamber to remove at least a portion of the residual fluid from the intermediate transfer line. The process may include directing the residual fluid flushed from the intermediate transfer line to another transfer line that is not a transfer line of the purification zone to restrict the residual fluid from being introduced into the purification zone.

Abstract: In a process for separating components in a feed stream by simulated countercurrent adsorptive separation, the process according to various aspects includes withdrawing an extract stream through one transfer line that contains residual fluid away from the adsorptive separation chamber. The process also includes directing an initial portion of the extract stream, including at least a portion of the residual fluid withdrawn through the one transfer line toward a first destination. The process further includes directing a subsequent portion of the extract stream withdrawn through the one transfer line toward a second destination.

Abstract: A process according to various approach includes flushing an intermediate transfer line between the first intermediate transfer line and the extract stream transfer line away from the adsorptive separation chamber to remove residual fluid from intermediate transfer line. The process may include directing the residual fluid flushed from the intermediate transfer line to a recycle stream to introduce the residual fluid into the adsorptive separation chamber.

Abstract: A process according to various approaches includes withdrawing the raffinate stream through one transfer line that contains residual fluid away from the adsorptive separation chamber. The process includes directing an initial portion of the raffinate stream, including at least a portion of the residual fluid, toward a first destination and directing a subsequent portion of the raffinate stream withdrawn through the one transfer line toward a second destination.

Abstract: The present invention is for high permeance and high selectivity blend polymeric membranes comprising poly(ethylene glycol) (PEG) and a highly permeable polymer selected from the group consisting of polymers of intrinsic microporosity (PIMs), tetrazole-functionalized polymers of intrinsic microporosity (TZPIMs), or mixtures thereof. The present invention also involves the use of such membranes for separations of liquids and gases.