Abstract: The present disclosure is directed to 1,3-butadiene extraction and steam cracking recovery systems, more particularly, to systems and methods for removing tar from the solvent loop of such systems using a membrane.

Abstract: A method can include: in a heat exchanger, cooling a biocrude oil emulsion stream received from a biocrude oil emulsion source, wherein the emulsion can include a biocrude oil phase, an aqueous phase, and solids; in a first mixing vessel, mixing the emulsion with a solvent to dissolve the biocrude oil phase and form a biocrude-solvent solution; in a first separator assembly, separating the biocrude-solvent solution from the aqueous phase and the solids; in a solvent recovery apparatus, recovering solvent from the biocrude-solvent solution; in a second mixing vessel, mixing the solvent with the aqueous phase and the solids received from the first separator assembly to dissolve biocrude oil remaining in the aqueous phase and the solids; and supplying the solvent and biocrude oil to the first mixing vessel as the solvent. In some examples, such a method can more effectively separate biocrude oil from the emulsion than conventional techniques.

Abstract: A hydrothermal liquefaction (HTL) reactor system can comprise a biomass slurry source, a mixing vessel, a pump, a HTL reactor section, a pressure letdown valve, and a vapor-liquid disengagement vessel. The mixing vessel can mix a biomass slurry stream received from the biomass slurry source with a vaporized water and gas byproducts stream. The pump can pressurize a biomass slurry stream received from the mixing vessel. The HTL reactor section can produce a product mixture stream from a biomass slurry stream received from the pump. The pressure letdown valve can reduce the pressure of a product mixture stream received from the HTL reactor section. The vapor-liquid disengagement vessel can separate vaporized water and gas byproducts from a product mixture stream received from the pressure letdown valve, wherein the separated vaporized water and gas byproducts can form the vaporized water and gas byproducts stream received by the mixing vessel.

Abstract: A hydrothermal liquefaction (HTL) system has a biomass slurry flow path with a first pump and a first heat exchanger network downstream of the first pump. The first heat exchanger network includes plurality of heat exchangers in a parallel, series, and/or series-parallel flow arrangement. The biomass slurry flow path extends through cold flow sides of the heat exchangers of the first heat exchanger network. The biomass slurry flow path includes a second pump downstream of the first heat exchanger network, and a second heat exchanger network downstream of the second pump. The biomass slurry flow path extends through cold flow sides of the heat exchangers of the second heat exchanger network. A hydrothermal liquefaction (HTL) reactor is downstream of the second heat exchanger network. Heat transfer liquid in a heat transfer liquid circuit flows through hot flow sides of the heat exchangers of the second heat exchanger network.

Abstract: A method can include: in a heat exchanger, cooling a biocrude oil emulsion stream received from a biocrude oil emulsion source, wherein the emulsion can include a biocrude oil phase, an aqueous phase, and solids; in a first mixing vessel, mixing the emulsion with a solvent to dissolve the biocrude oil phase and form a biocrude-solvent solution; in a first separator assembly, separating the biocrude-solvent solution from the aqueous phase and the solids; in a solvent recovery apparatus, recovering solvent from the biocrude-solvent solution; in a second mixing vessel, mixing the solvent with the aqueous phase and the solids received from the first separator assembly to dissolve biocrude oil remaining in the aqueous phase and the solids; and supplying the solvent and biocrude oil to the first mixing vessel as the solvent. In some examples, such a method can more effectively separate biocrude oil from the emulsion than conventional techniques.

Abstract: Processes and systems for stabilizing the operation of a steam cracker primary fractionator. In some embodiments, the process can include (I) feeding a first steam cracker effluent into a steam cracker primary fractionator. The process can also include (II) feeding a make-up liquid stream into the steam cracker primary fractionator. The process can also include (III) recovering a steam cracker gas oil (“SCGO”) side stream from the steam cracker primary fractionator. The process can also include (IV) recovering a steam cracker tar (“SCT”) stream from a location at and/or in the vicinity of a bottom of the primary fractionator. The make-up liquid stream can include a first hydrocarbon portion and a second hydrocarbon portion. The first hydrocarbon portion can be distributed into the SCGO side stream. The second hydrocarbon portion can be distributed into the SCT stream.

Abstract: The present disclosure is directed to 1,3-butadiene extraction and steam cracking recovery systems, more particularly, to systems and methods for removing tar from the solvent loop of such systems using a membrane.

Abstract: A hydrothermal liquefaction (HTL) system has a biomass slurry flow path with a first pump and a first heat exchanger network downstream of the first pump. The first heat exchanger network includes plurality of heat exchangers in a parallel, series, and/or series-parallel flow arrangement. The biomass slurry flow path extends through cold flow sides of the heat exchangers of the first heat exchanger network. The biomass slurry flow path includes a second pump downstream of the first heat exchanger network, and a second heat exchanger network downstream of the second pump. The biomass slurry flow path extends through cold flow sides of the heat exchangers of the second heat exchanger network. A hydrothermal liquefaction (HTL) reactor is downstream of the second heat exchanger network. Heat transfer liquid in a heat transfer liquid circuit flows through hot flow sides of the heat exchangers of the second heat exchanger network.

Abstract: Processes and systems for upgrading a hydrocarbon-containing feed. The hydrocarbon containing feed and a plurality of fluidized particles can be fed into a pyrolysis reaction zone. The plurality of fluidized particles can have a first temperature that can be sufficiently high to enable pyrolysis of at least a portion of the hydrocarbon-containing feed on contacting the particles. The particles can include an oxide of a transition metal element capable of oxidizing molecular hydrogen at the first temperature. The hydrocarbon-containing feed can be contacted with the particles in the pyrolysis reaction zone to effect pyrolysis of at least a portion of the hydrocarbon-containing feed to produce a pyrolysis effluent. At least a portion of the transition metal element in the particles in the pyrolysis effluent can be at a reduced state compared to the transition metal element in the particles fed into the pyrolysis reaction zone.

Abstract: A method for reducing CO2 emissions from steam cracking operations can include: introducing an oxygen-rich stream comprising oxygen and from 0 wt % to 15 wt % nitrogen to a vessel; introducing hydrocarbon combustion fuel to the vessel; combusting oxygen and hydrocarbon combustion fuel in the vessel to (1) produce a flue gas comprising carbon dioxide and water and (2) heat a cracking coil passing through the vessel; and performing a steam cracking reaction in the cracking coil passing through the vessel.

Abstract: Systems and methods are provided for production of high octane hydrocarbon from an isoparaffin feed using oxidation acid catalysis chemistry.

Abstract: Systems and methods are provided for forming alkylate from a tertiary alcohol feed. Olefins for the alkylation reaction can be generated from a portion of the tertiary alcohol feed. The tertiary alcohol feed can be obtained, for example, by selective oxidation to convert a portion of an isoparaffin-containing feed into alcohol, such as conversion of isobutane to t-butyl alcohol. The alcohol can then be converted to an alkene, such as conversion of t-butyl alcohol to isobutene, in the alkylation reaction environment in the presence of a solid acid catalyst. The solid acid catalyst can then facilitate dimerization of the alkenes (e.g. isobutene) to form C8+ olefins (e.g. isooctene). A catalyst having an MWW framework is an example of a suitable solid acid catalyst.

Abstract: Systems and methods are provided for production of high octane hydrocarbon from an isoparaffin feed using oxidation acid catalysis chemistry.

Abstract: Systems and methods are provided for forming alkylate from a tertiary alcohol feed. Olefins for the alkylation reaction can be generated from a portion of the tertiary alcohol feed. The tertiary alcohol feed can be obtained, for example, by selective oxidation to convert a portion of an isoparaffin-containing feed into alcohol, such as conversion of isobutane to t-butyl alcohol. The alcohol can then be converted to an alkene, such as conversion of t-butyl alcohol to isobutene, in the alkylation reaction environment in the presence of a solid acid catalyst. The solid acid catalyst can then facilitate dimerization of the alkenes (e.g. isobutene) to form C8+ olefins (e.g. isooctene). A catalyst having an MWW framework is an example of a suitable solid acid catalyst.

Abstract: A process for removing cyclopentene from the C5 fraction of a light olefin feed useful in an isoparaffin/olefin alkylation process redistributes fragments of C5 olefins formed by ring opening metathesis (ROM) in the presence of a catalyst. The higher molecular weight olefins produced in the reaction can be blended into the gasoline blend pool without imposing a significant or any vapor pressure penalty. Cyclopentene present in the C5 portion of the feed undergoes various ring opening reactions while other pentenes are converted to hydrocarbon products of lower and higher molecular weight relative to pentene. The reduction in cyclopentene results in a reduced tendency for the formation of acid soluble oil (ASO) during alkylation.

Abstract: Method of determining a total HF concentration metric in an environment including measuring an uncorrected HF concentration metric in the environment based on a first infrared absorption measurement at a wavelength corresponding to a vibrational frequency of a non-hydrogen bonded gas phase HF molecule; determining an ambient H2O concentration metric in the environment available for reaction with the non-hydrogen bonded gas phase HF molecules at or about the time of obtaining the first infrared absorption measurement; calculating a HF hydrate concentration metric in the environment based on the uncorrected HF concentration metric, the ambient H2O concentration metric and a reaction equilibrium relationship between the non-hydrogen bonded gas phase HF molecule and the HF hydrate; and determining the total HF concentration metric in the environment based on the uncorrected HF concentration metric and an amount of HF determined by the HF hydrate concentration metric.

Abstract: Method of determining a total HF concentration metric in an environment including measuring an uncorrected HF concentration metric in the environment based on a first infrared absorption measurement at a wavelength corresponding to a vibrational frequency of a non-hydrogen bonded gas phase HF molecule; determining an ambient H2O concentration metric in the environment available for reaction with the non-hydrogen bonded gas phase HF molecules at or about the time of obtaining the first infrared absorption measurement; calculating a HF hydrate concentration metric in the environment based on the uncorrected HF concentration metric, the ambient H2O concentration metric and a reaction equilibrium relationship between the non-hydrogen bonded gas phase HF molecule and the HF hydrate; and determining the total HF concentration metric in the environment based on the uncorrected HF concentration metric and an amount of HF determined by the HF hydrate concentration metric.