Abstract: A process of producing ethylene and propylene from naphtha, the process comprising: producing light paraffins—ethane, hydrogen/methane/residual ethane and propane rich streams—in a dividing wall fractionation column from a stream of hydrogen, methane, propane, and residual C4+ produced in the reactor section of a naphtha-to-ethane-and-propane processing unit by reacting naphtha with hydrogen, a naphtha reactor effluent stream produced by a naphtha reactor of the naphtha-to-ethane-and-propane processing unit is cooled to produce a feed stream. The feed stream is passed to a dividing wall fractionation column. An ethane stream from the dividing wall fractionation column is passed to an ethane steam cracker to produce a cracking heater effluent stream. The cracking heater effluent stream is passed to a coldbox of the ethane steam cracker after multiple steps such as quenching, compression, cooling, caustic scrubbing, drying.

Abstract: In a process of producing ethylene and propylene from naphtha the process a feed stream comprising hydrogen, methane, ethane, and propane and residual C4+ from a naphtha-to-ethane-and-propane reactor is fed to a dividing wall fractionation column.

Abstract: A process and apparatus integrate recovery of propylene from a pyrolysis reactor and a paraffin dehydrogenation reactor. A common depropanizer fractionates propane feed and pyrolysis reactor effluent to provide a C3 stream. A dividing wall may be used in the column to prevent cross contamination by the pyrolysis effluent with the propane dehydrogenation feed.

Abstract: A process and apparatus integrate recovery of propylene from a pyrolysis reactor and a paraffin dehydrogenation reactor. A common C3 splitter column fractionates propylene product from propane recycle to a paraffin dehydrogenation reactor. The C3 hydrocarbons may be provided from a pyrolysis reactor and from a dehydrogenation reactor.

Abstract: A process and apparatus integrate recovery of propylene from a pyrolysis reactor and a paraffin dehydrogenation reactor. The improved process for recovering light olefins utilizes heats of compression to heat reboil streams.

Abstract: A process and apparatus integrate recovery of propylene from a pyrolysis reactor and a paraffin dehydrogenation reactor. A stripping column for fractionating a dehydrogenation stream is coupled with a demethanizer column for fractionating a pyrolyzed stream. The stripping overhead stream comprising C2? hydrocarbons are fractionated with the pyrolyzed stream in the demethanizer column. The coupling omits the need for a conventional deethanizer column and separate refrigeration system in the propane dehydrogenation unit.

Abstract: A process and apparatus cool a pyrolyzed stream and a dehydrogenated stream in respective cold boxes by use of a refrigerant compressed with a common compressor. The refrigerant is compressed and used to cool a pyrolysis cold box and a dehydrogenation cold box.

Abstract: Embodiments of apparatuses and methods for reforming of hydrocarbons including recovery of products are provided. In one example, a method comprises separating a reforming-zone effluent into a net gas phase stream and a liquid phase hydrocarbon stream. The net gas phase stream is separated for forming an H2-rich stream and a first liquid phase hydrocarbon stream. The H2-rich stream may be contacted with an adsorbent to form an H2-ultra rich stream and a gas stream. C3/C4 hydrocarbons are absorbed from the gas stream with the liquid phase hydrocarbon stream. The gas stream may be contacted with an H2/hydrocarbon separation membrane to separate the PSA tail gas stream and form an H2-rich permeate stream and an H2 depleted non-permeate residue stream.

Abstract: Embodiments of apparatuses and methods for reforming of hydrocarbons including recovery of products are provided. In one example, a method comprises separating a reforming-zone effluent into a net gas phase stream and a liquid phase hydrocarbon stream. The net gas phase stream is separated for forming an H2-rich stream and a first liquid phase hydrocarbon stream. The H2-rich stream may be contacted with an adsorbent to form an H2-ultra rich stream and a gas stream. C3/C4 hydrocarbons are absorbed from the gas stream with the liquid phase hydrocarbon stream. The gas stream may be contacted with an H2/hydrocarbon separation membrane to separate the PSA tail gas stream and form an H2-rich permeate stream and an H2 depleted non-permeate residue stream.