Abstract: Systems and processes for the efficient conversion of high concentration isoolefin streams to tertiary alkyl ethers are disclosed. The systems and processes may include a feed system to advantageously divide the high concentration isoolefin feed to multiple fixed bed reactors and a catalytic distillation reactor to control the reaction exotherm and achieve a high isoolefin conversion.

Abstract: A process for the selective dimerization and etherification of isoolefins. The process including feeding a mixed C5 stream to a selective hydrogenation unit to convert dienes to olefins and isoolefins, producing a hydrogenated effluent stream. The hydrogenated effluent stream is fed to a first fixed bed reactor, producing a first reactor effluent. The first reactor effluent is fed to a catalytic distillation reactor system, producing a first overheads including unreacted olefins, isoolefins, oxygenate, and one or more C5 ethers and a first bottoms including dimers of the isoolefins, any produced trimers of the isoolefins, and heavy oxygenates. The first overheads is fed to a second fixed bed reactor, producing a second reactor effluent including dimers of the isoolefins, unreacted C5s, and unreacted oxygenates.

Abstract: There are disclosed processes and systems wet air oxidation systems and processes which provide for the combined treatment of a spent caustic with a spent material (e.g., spent carbon, spent biological material, or combinations thereof) to produce a regenerated spent material stream.

Abstract: Systems and processes for the production of a high purity isobutylene stream, a high purity isooctene stream or for the co-production of a high purity isobutylene and a high purity isooctene. The systems and processes advantageously process mixed C4 hydrocarbon streams via etherification, back cracking, isomerization, and/or dimerization, along with various separation systems, to produce the desired high purity streams.

Abstract: An apparatus including a radiant heating section and a flue gas stack; one or more process coils disposed within the radiant heating section; one or more fuel-fired burners disposed within the radiant heating section, the one or more fuel-fired burners configured for combusting a fuel and producing the combustion gas; one or more electrical heating elements disposed within the radiant heating section, the one or more electrical heating elements arranged to provide a second radiant energy to a lower elevation of the one or more process coils; and an internal baffle located at an elevation between the upper elevation and the lower elevation, the internal baffle arranged to provide shielding of the one or more electrical heating elements from flame and combustion gases from the one or more fuel-fired burners.

Abstract: There are provided systems (10) and processes for the selective removal of cyanide from a wastewater stream (12) comprising cyanide and an amount of organic compounds therein.

Abstract: Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker.

Abstract: Electrical heater systems including one or multiple electrical heaters and a stack for combusting materials leaked into and vented from the electrical heaters. Configurations may include fluid conduits, pressure doors and other equipment for controlling a flow of leaked process fluid between the heater enclosure and the stack. Configurations may also include a purge gas distribution system for purging heater enclosures and preventing thermal shock of electrical heating elements.

Abstract: An apparatus for heating petroleum, petrochemical, chemical process fluids, and boiler feed water or steam generation with a combination, or individual operation, of electrical elements and fired burners. The apparatus includes a radiant heating section and a flue gas stack for exhausting a combustion gas to the atmosphere. The radiant section includes one or more process coils, one or more fuel-fired burners for combusting a fuel and producing the combustion gas, where the one or more fuel-fired burners are arranged to provide radiant energy to a first area of the one or more process coils, and one or more electrical heating elements arranged to provide radiant energy to a second area of the one or more process coils. The one or more electrical heating elements are configured to provide 5% or more of a combined maximum energy output of the fuel-fired burners and the electrical heating elements.

Abstract: Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker.

Abstract: A process for producing olefins may include dehydrogenating a first alkane in a first reactor to produce a first effluent comprising at least one of a first n-olefin or a first diolefin; removing the first effluent from the first reactor; and regenerating the first reactor. The first reactor may include a first dehydrogenation catalyst and a first phase change material.

Abstract: Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into light and heavy fractions utilizing convection heat from heaters used in steam cracking. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize either an ebullated bed reactor with extrudate catalysts or a slurry hydrocracking reactor using a homogeneous catalyst system, such as a molybdenum based catalysts which may optionally be promoted with nickel. Products from the upgrading operations can be finished olefins and/or aromatics, or, for heavier products from the upgrading operations, may be used as feed to the steam cracker.

Abstract: Embodiments disclosed herein relate to systems and processes for producing olefins and/or dienes. The systems and processes may include thermally cracking a C1-C4 hydrocarbon containing feed to produce a cracked hydrocarbon effluent containing a mixture of olefins and paraffins. The systems and processes may also include dehydrogenating the cracked hydrocarbon effluent to produce a dehydrogenated hydrocarbon effluent containing additional olefins and/or dienes.

Abstract: A system for steam cracking a whole crude that may include a volatilization device, a control system, a separator, and a steam pyrolysis reactor. The volatilization device may be configured to separate a vapor phase from a liquid phase. The control system may be configured to maintain a flow rate of the whole crude and steam, at an initial relative velocity of less than 30 m/s. The separator may be fluidly connected to the volatilization device and configured to separate the liquid phase into a second vapor phase, and a second liquid phase. The steam pyrolysis reactor may include a convection section and a steam pyrolysis heater section, the convection section configured to heat the vapor phase, the liquid phase, and the second vapor phase, and the steam pyrolysis heater section configured to steam crack hydrocarbons in the vapor phase thereby generating a cracked hydrocarbon product.

Abstract: Systems and methods for the production of a high purity isoamylene product. The isoamylene in a mixed hydrocarbon stream may initially be converted to TAME via etherification, and a subsequent decomposition of the TAME may result in a high purity isoamylene stream with very low impurities that is suitable for a variety of petrochemical applications, such as for use in the production of fragrances, pesticides, peroxides, polymer antioxidants, UV stabilizers and hydrocarbon resins.

Abstract: Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker.

Abstract: A heat exchanger assembly including an elongated tubular heat exchanger enclosure defining an interior chamber. A tube sheet is positioned within the interior chamber of the heat exchanger enclosure separating the interior chamber into a shell side and a channel side. The interior portion is configured to removably receive a tube bundle positioned within the shell side of the interior chamber. An annular sleeve member is positioned within the channel side of the interior chamber of the heat exchanger enclosure. An annular elastic torsion member is positioned within the channel side of the interior chamber of the heat exchanger such that the sleeve member is positioned between the tube sheet and the elastic torsion member. The elastic torsion member has an inner circumference deflectable relative to its outer circumference for torsioning the elastic torsion member.

Abstract: Systems and processes for the treatment of a naphtha range hydrocarbon feedstock comprising sulfur-containing compounds, nitrogen-containing compounds, olefins, diolefins, and aromatics. The systems and processes are configured to treat the naphtha range hydrocarbon feedstock to convert the sulfur-containing compounds, nitrogen-containing compounds, and olefins, diolefins while less than 2 wt % aromatics are hydrogenated, producing an olefin lean overheads fraction comprising less than 0.2 wt % olefins and less than 100 mg/kg sulfur and an aromatics rich fraction comprising less than 50 ppmw olefins, less than 0.5 ppmw sulfur and less than 0.5 ppmw nitrogen.

Abstract: A process for dehydrogenating a paraffinic feedstock, producing olefins and/or dienes. The process includes feeding a paraffinic hydrocarbon feedstock comprising one or more C2+ paraffinic hydrocarbons and a fuel gas stream to a dehydrogenation reactor preheater, combusting the fuel gas stream in the dehydrogenation reactor preheater and heating the paraffinic hydrocarbon feedstock to a temperature in the range of 500-650° C., producing a heated paraffinic feedstock, feeding the heated paraffinic feedstock to a first dehydrogenation reactor operating in a reaction mode and containing an active dehydrogenation catalyst and at least one first electrical heating element, heating the heated paraffinic feedstock in the first dehydrogenation reactor using the at least one first electrical heating element, and contacting the heated paraffinic feedstock with the active dehydrogenation catalyst and the at least one electrical heating element thereby producing an olefinic product stream comprising one or more olefins.

Abstract: Systems and processes for converting light or very light sweet crudes and condensates to chemicals and petrochemicals. The process includes providing a hydrocarbon feedstock comprising a crude oil or condensate having an API gravity of at least 35, a sulfur content of less than 0.2 wt %, and less than 10 wt % of hydrocarbons having a normal boiling point above 575° C. The hydrocarbon feedstock is heated and separated to recover a light fraction, a middle fraction, and optionally a heavy fraction. The light fraction is steam cracked to produce a cracked light fraction and the middle fraction is separately steam cracked to produce a cracked middle fraction. The cracked light fraction and the cracked middle fraction are then separated to recover one or more product fractions including an ethylene fraction and a propylene fraction.