Abstract: The present disclosure relates to aggregating and sharing wellness data. The wellness data can be received by a user device from any number of sensors external or internal to the user device, from a user manually entering the wellness data, or from other users or entities. The user device can securely store the wellness data on the user device and transmit the wellness data to be stored on a remote database. A user of the device can share some or all of the wellness data with friends, relatives, caregivers, healthcare providers, or the like. The user device can further display a user's wellness data in an aggregated view of different types of wellness data. Wellness data of other users can also be viewed if authorizations from those users have been received.

Abstract: Systems and methods are provided for conversion of polymers (such as plastic waste) to olefins. The systems and methods can include a recycle loop so that a portion of the pyrolysis effluent can be combined with solid plastic feedstock. The input flow to the pyrolysis reactor can correspond to a slurry of plastic particles in recycled effluent or a solution of plastic in recycled effluent.

Abstract: Systems and methods are provided for conversion of polymers (such as plastic waste) to olefins. The systems and methods can include an initial pyrolysis stage where a plastic feedstock is delivered to the initial pyrolysis stage by one or more melt extruders. The one or more melt extruders can be heated to maintain the plastic feedstock in a liquid state during delivery of the plastic feedstock to the initial pyrolysis stage. This can allow for delivery of the plastic feedstock into the pyrolysis process with a controlled distribution of plastic into the pyrolysis reactor.

Abstract: Processes and systems for upgrading a hydrocarbon feed. The process can include feeding a hydrocarbon feed, catalyst particles, and molecular hydrogen (H2) into a separation zone. The hydrocarbon feed and H2 can be contacted in the presence of the catalyst particles under hydrotreating conditions in the separation zone that can include contacting under a total pressure of less than 3,500 kilopascals-gauge. The H2 can be fed into the separation zone at a rate of no greater than 270 cubic meters of H2 per cubic meter of the hydrocarbon feed, where the volume of H2 and hydrocarbon feed are based on a temperature of 25 C and a pressure of 101 kilopascals-absolute. A vapor phase hydrocarbon stream and a liquid phase hydrocarbon stream can be obtained from the separation zone. At least a portion of the vapor phase hydrocarbon stream can be fed into a pyrolysis reaction zone to produce a pyrolysis effluent.

Abstract: A method for washing an oligomerization reactor using by-product solvent recovered from the reactor can include: catalytically converting a monomer in a reactor section in a reaction mode in the presence of a catalyst to form a product stream comprising an oligomer, a by-product solvent, and a polymeric by-product; separating the product stream into a first fraction comprising the oligomer and a second fraction comprising a mixture of the by-product solvent and the polymeric by-product; and separating, in a thin film evaporator, the second fraction into a third fraction comprising the by-product solvent and a fourth fraction comprising the polymeric by-product.

Abstract: Processes and systems for upgrading a hydrocarbon feed. The process can include feeding a hydrocarbon feed, catalyst particles, and molecular hydrogen (H2) into a separation zone. The hydrocarbon feed and H2 can be contacted in the presence of the catalyst particles under hydrotreating conditions in the separation zone that can include contacting under a total pressure of less than 3,500 kilopascals-gauge. The H2 can be fed into the separation zone at a rate of no greater than 270 cubic meters of H2 per cubic meter of the hydrocarbon feed, where the volume of H2 and hydrocarbon feed are based on a temperature of 25 C and a pressure of 101 kilopascals-absolute. A vapor phase hydrocarbon stream and a liquid phase hydrocarbon stream can be obtained from the separation zone. At least a portion of the vapor phase hydrocarbon stream can be fed into a pyrolysis reaction zone to produce a pyrolysis effluent.

Abstract: A method for washing an oligomerization reactor using by-product solvent recovered from the reactor can include: catalytically converting a monomer in a reactor section in a reaction mode in the presence of a catalyst to form a product stream comprising an oligomer, a by-product solvent, and a polymeric by-product; separating the product stream into a first fraction comprising the oligomer and a second fraction comprising a mixture of the by-product solvent and the polymeric by-product; and separating, in a thin film evaporator, the second fraction into a third fraction comprising the by-product solvent and a fourth fraction comprising the polymeric by-product.

Abstract: The present disclosure provides assemblies for producing linear alpha olefins and methods for producing linear alpha olefins. In at least one embodiment, a method for producing a linear alpha olefin includes oligomerizing an olefin in the presence of a catalyst and a process solvent in at least one reactor, quenching the reactor effluent, and subjecting the quenched effluent to separation steps to obtain a stream enriched in one or more linear alpha olefins.

Abstract: The process involves the use of two rotary valves to implement Varicol operation of a simulated moving bed apparatus to separate a product from at least one multicomponent feed. In a particular embodiment, paraxylene is separated from a mixture of C8 aromatic hydrocarbons. The use of the Varicol process further enhances the separation of the desired product and provides flexibility with a simulated moving bed apparatus using dual rotary valves.

Abstract: A process for oligomerizing an olefin feedstock to produce an olgiomerization product, a method for analysing an oligomerization product, and an oligomerization product are disclosed. Preferably, the process comprises contacting the olefin feedstock with an oligomerization catalyst under effective oligomerization conditions, wherein the olefin feedstock comprises at least 50 wt % of one or more C6 olefins, based on the weight of the olefins in the olefin feedstock, and wherein the oligomerization catalyst comprises a crystalline molecular sieve, such as an intermediate pore size crystalline molecular sieve or a large pore size crystalline molecular sieve.

Abstract: The present disclosure provides assemblies for producing linear alpha olefins and methods for producing linear alpha olefins. In at least one embodiment, a method for producing a linear alpha olefin includes providing an olefin, a catalyst, and a process solvent to a reactor under oligomerization conditions; obtaining an effluent produced in the reactor; transferring the effluent through an effluent line; and providing a quench agent to the effluent line via a quench agent line coupled with the effluent line. In at least one embodiment, an assembly for producing linear alpha olefins includes a configuration to provide olefin, catalyst and process solvent coupled with a reactor; an effluent line coupled with the reactor at a first end and coupled with a mixer or a flash drum at a second end; and a quench agent line coupled with the effluent line at a first end.

Abstract: The present disclosure provides assemblies for producing linear alpha olefins and methods for producing linear alpha olefins. In at least one embodiment, a method for forming a linear alpha olefin, includes providing an olefin, a catalyst, and a process solvent to a reactor; obtaining an effluent from the reactor; and transferring the effluent to a distillation tower comprising a dividing wall. In at least one embodiment, an assembly for producing linear alpha olefins includes a distillation tower comprising a dividing wall having a height that is from 25% to 95% of the height of the distillation tower. In at least one embodiment, a method for forming a linear alpha olefin comprises providing an olefin, a catalyst, and orthoxylene to a tubular reactor; obtaining an effluent from the tubular reactor; and transferring the effluent to a distillation tower.

Abstract: The present disclosure provides assemblies for producing linear alpha olefins and methods for producing linear alpha olefins. In at least one embodiment, a method for producing a linear alpha olefin includes providing an olefin, a catalyst, and a process solvent to a reactor under oligomerization conditions; obtaining an effluent produced in the reactor; and transferring the effluent to a solvent-containing portion of a flash drum via a first effluent line coupled with the flash drum. In at least one embodiment, an assembly for producing linear alpha olefins includes a configuration to provide olefin, catalyst and process solvent coupled with a reactor; a flash drum; a first effluent line coupled with the reactor at a first end and coupled with the flash drum at a second end; and a second effluent line coupled with the flash drum at a first end and coupled with the first effluent line at a second end.

Abstract: The present disclosure provides assemblies for producing linear alpha olefins and methods for producing linear alpha olefins. In at least one embodiment, a method for producing a linear alpha olefin includes providing an olefin, a catalyst, and a process solvent to a first tubular reactor; obtaining an effluent from the first tubular reactor; and transferring the effluent to a second tubular reactor. In at least one embodiment, an assembly for producing linear alpha olefins includes a first tubular reactor having a first end and a second end; an effluent line having a first end and a second end, the first end coupled with the second end of the first tubular reactor; and a second tubular reactor having a first end and a second end, the first end coupled with the second end of the effluent line.

Abstract: A process to separate paraxylene from a mixture of paraxylene, metaxylene, orthoxylene, and ethylbenzene in a commercial simulated moving bed apparatus in a reduced number of beds is provided, allowing an additional separation to be conducted in the remaining beds. This additional separation may separate another xylene isomer, ethylbenzene, or a non-aromatic C8+ hydrocarbon from the raffinate stream produced by the first separation. A PowerFeed process is used to recover paraxylene in a first adsorption zone containing 8-16 beds of a conventional 24-bed simulated moving bed adsorption apparatus, and then a second separation may be conducted in a second adsorption zone containing the remaining beds.

Abstract: Disclosed is a process for recovering paraxylene in which a first simulated moving bed adsorption unit is used to produce two extract streams—one rich in paraxylene and a paraxylene-rich extract stream that is lean in ethylbenzene and an ethylbenzene-rich extract stream that is lean in paraxylene- and a paraxylene-depleted raffinate stream. A significant amount of the ethylbenzene is removed in the ethylbenzene-rich extract stream (at least enough to limit buildup in the isomerization loop), so the paraxylene-depleted raffinate stream may be isomerized in the liquid phase. Avoiding vapor phase isomerization saves energy and capital, as liquid phase isomerization requires less energy and capital than the vapor phase isomerization process due to the requirement of vaporizing the paraxylene-depleted stream and the use of hydrogen, which requires an energy and capital intensive hydrogen recycle loop.

Abstract: A process to separate paraxylene from a mixture of paraxylene, metaxylene, orthoxylene, and ethylbenzene in a commercial simulated moving bed apparatus in a reduced number of beds is provided, allowing an additional separation to be conducted in the remaining beds. This additional separation may separate another xylene isomer, ethylbenzene, or a non-aromatic C8+ hydrocarbon from the raffinate stream produced by the first separation. A PowerFeed process is used to recover paraxylene in a first adsorption zone containing 8-16 beds of a conventional 24-bed simulated moving bed adsorption apparatus, and then a second separation may be conducted in a second adsorption zone containing the remaining beds.

Abstract: The process involves the use of two rotary valves to implement Varicol operation of a simulated moving bed apparatus to separate a product from at least one multicomponent feed. In a particular embodiment, paraxylene is separated from a mixture of C8 aromatic hydrocarbons. The use of the Varicol process further enhances the separation of the desired product and provides flexibility with a simulated moving bed apparatus using dual rotary valves.

Abstract: A process for selective oxidation of dimethyl-1,1?-biphenyl to form methyl-1,1?-biphenyl mono-carboxylic acid(s), comprising contacting a solution of dimethyl-1,1?-biphenyl in acetic acid solvent in the presence of a Co(II) acetate catalyst and air, and optionally adding a co-solvent, or adding sodium or potassium acetate, and oxidizing the dimethyl-1,1?-biphenyl under time and temperature conditions sufficient to form one or more methyl-1,1?-biphenyl mono-carboxylic acid(s). The mono-carboxylic acids are advantageously isolated and esterified to form biphenyl mono-esters for use as plasticizers.

Abstract: Disclosed herein are processes for recovering paraxylene in which a first simulated moving bed adsorption unit is used to produce a paraxylene-rich extract stream that also contains a significant amount of the ethylbenzene and a paraxylene-depleted raffinate stream. Because a significant amount of the ethylbenzene is removed in the paraxylene-rich extract stream (at least enough to limit buildup in the isomerization loop), the paraxylene-depleted raffinate stream may be isomerized in the liquid phase. Avoiding vapor phase isomerization saves energy and capital, as liquid phase isomerization requires less energy and capital than the vapor phase isomerization process due to the requirement of vaporizing the paraxylene-depleted stream and the use of hydrogen, which requires an energy- and capital-intensive hydrogen recycle loop.