Abstract: Systems and methods for separating a mixture comprising C4 hydrocarbons and a solvent have been disclosed. The mixture is produced as a bottom stream of a rectifier column. The mixture is processed in at least two heating and flash-evaporating cycles to remove at least some C4 hydrocarbons as vapor streams. The resulted liquid stream is further degassed in a degasser column to produce a recycle vapor stream and a lean solvent stream.

Abstract: Systems and methods for separating a mixture comprising C4 hydrocarbons and a solvent have been disclosed. The mixture is produced as a bottom stream of a rectifier column. The mixture is processed in at least two heating and flash-evaporating cycles to remove at least some C4 hydrocarbons as vapor streams. The resulted liquid stream is further degassed in a degasser column to produce a recycle vapor stream and a lean solvent stream.

Abstract: Systems and methods for producing dicyclopentadiene via thermal dimerization of cyclopentadiene. The feed stream comprising cyclopentadiene is flowed through four shell and tube heat exchangers in series. Each of the shell and tube heat exchangers comprise a shell and one or more tubes disposed in the shell. The feed stream is flowed in the tubes while the heat transfer medium is flowed in the shell to absorb the exothermic heat released by the dimerization of cyclopentadiene in the tubes. In this way, the temperature in the tubes is controlled at a level where the conversion rate of cyclopentadiene is above 99% and the occurrence of runaway reaction is substantially prevented.

Abstract: Methods and systems for producing light olefins are disclosed. A feedstock comprising crude oil is distilled to produce a plurality of streams including a naphtha stream and a vacuum residue stream. The naphtha is fed to a steam cracking unit to produce light olefins, C4 hydrocarbons, pyrolysis gasoline and pyrolysis oil. The vacuum residue stream is hydrocracked to produce additional naphtha and heavy unconverted oil. The heavy unconverted oil and the pyrolysis oil from steam cracking unit can be deasphalted to produce deasphalted oil and pitch product. The deasphalted oil can be further hydrocracked to produce naphtha. The pitch product can be gasified to produce synthesis gas, which is further used to produce methanol. The methanol can be used to react with isobutylene of the C4 hydrocarbon stream from steam cracker to produce methyl tert-butyl ether (MTBE).

Abstract: Methods and systems for producing light olefins are disclosed. A feedstock comprising crude oil is distilled to produce a plurality of streams including a naphtha stream and a vacuum residue stream. The naphtha is fed to a steam cracking unit to produce light olefins, C4 hydrocarbons, pyrolysis gasoline and pyrolysis oil. The vacuum residue stream is hydrocracked to produce additional naphtha and heavy unconverted oil. The heavy unconverted oil and the pyrolysis oil from steam cracking unit can be deasphalted to produce deasphalted oil and pitch product. The deasphalted oil can be further hydrocracked to produce naphtha. The pitch product can be gasified to produce synthesis gas, which is further used to produce methanol. The methanol can be used to react with isobutylene of the C4 hydrocarbon stream from steam cracker to produce methyl tert-butyl ether (MTBE).

Abstract: Systems and methods for producing dicyclopentadiene via thermal dimerization of cyclopentadiene. The feed stream comprising cyclopentadiene is flowed through four shell and tube heat exchangers in series. Each of the shell and tube heat exchangers comprise a shell and one or more tubes disposed in the shell. The feed stream is flowed in the tubes while the heat transfer medium is flowed in the shell to absorb the exothermic heat released by the dimerization of cyclopentadiene in the tubes. In this way, the temperature in the tubes is controlled at a level where the conversion rate of cyclopentadiene is above 99% and the occurrence of runaway reaction is substantially prevented.

Abstract: Methods and systems for separating C3 hydrocarbons from lighter hydrocarbons, carbon monoxide, carbon dioxide, and water are provided. In certain embodiments, the methods include feeding a gaseous mixture including C1, C2, and C3 hydrocarbons and benzene solvent to the absorber column where benzene solvent selectively absorbs C3 hydrocarbons. The methods can further include removing a first stream comprising benzene solvent and absorbed C3 hydrocarbons from the absorber column, and feeding the first stream to a stripper column where benzene solvent is separated from C3 hydrocarbons, and removing a second stream comprising C3 hydrocarbons from the stripper column.

Abstract: Methods and systems for treating pygas are disclosed. Methods include depentanizing the pygas to produce a C5 stream and a C6+ stream before hydrotreating the C6+ stream, to integrate the processing of pygas with the production of isoprene, piperylene, and dicyclopentadiene. Systems include a depentanizer added before a pygas hydrotreatment unit.

Abstract: Methods and systems for recovering dicyclopentadiene from pygas are provided. Methods can include heating pygas to generated heated pygas, recovering a C5 fraction from the heated pygas, and dimerizing cyclopentadiene from the C5 fraction to form dicyclopentadiene. Methods can further include recovering the C5 fraction from the pygas in a depentanizer column. Other methods can include heating pygas including dicyclopentadiene to form cyclopentadiene and hydrogenating cyclopentadiene in the pygas to form cyclopentane.

Abstract: The present disclosure provides methods and system for the cooling of process plant water. A system can include a first heat exchanger for exchanging heat between a first process water stream and a refrigerant; a multiphase pump, coupled to the first heat exchanger, to increase the pressure of the refrigerant; a second heat exchanger, coupled to the multiphase pump and the first heat exchanger, for exchanging heat between a second process water stream and the refrigerant; a first expansion valve, coupled to the second heat exchanger, for lowering the temperature of the refrigerant; a vapor-liquid separator, coupled to the first expansion valve and the multiphase pump, for separating the liquid and vapor phases of the refrigerant; and a second expansion valve, coupled to the vapor-liquid separator and the first heat exchanger, for lowering the temperature of the liquid phase of the refrigerant.

Abstract: Methods and systems for recovering dicyclopentadiene from pygas are provided. Methods can include heating pygas to generated heated pygas, recovering a C5 fraction from the heated pygas, and dimerizing cyclopentadiene from the C5 fraction to form dicyclopentadiene. Methods can further include recovering the C5 fraction from the pygas in a depentanizer column. Other methods can include heating pygas including dicyclopentadiene to form cyclopentadiene and hydrogenating cyclopentadiene in the pygas to form cyclopentane.

Abstract: Methods and systems for separating C3 hydrocarbons from lighter hydrocarbons, carbon monoxide, carbon dioxide, and water are provided. In certain embodiments, the methods include feeding a gaseous mixture including C1, C2, and C3 hydrocarbons and benzene solvent to the absorber column where benzene solvent selectively absorbs C3 hydrocarbons. The methods can further include removing a first stream comprising benzene solvent and absorbed C3 hydrocarbons from the absorber column, and feeding the first stream to a stripper column where benzene solvent is separated from C3 hydrocarbons, and removing a second stream comprising C3 hydrocarbons from the stripper column.

Abstract: Methods and systems for treating pygas are disclosed. Methods include depentanizing the pygas to produce a C5 stream and a C6+ stream before hydrotreating the C6+ stream, to integrate the processing of pygas with the production of isoprene, piperylene, and dicyclopentadiene. Systems include a depentanizer added before a pygas hydrotreatment unit.

Abstract: A process for extracting isoprene from a pyrolysis gas mixture or a C5 fraction wherein isoprene is purified by plural extractive distillations in the presence of a polar solvent and cyclopentadiene is effectively removed and recycled as a feedstock without being converted into its dimer, dicyclopentadiene. The isoprene recovered from the process described is more than 99.5% pure.

Abstract: A process for extracting isoprene from a pyrolysis gas mixture or a C5 fraction wherein isoprene is purified by plural extractive distillations in the presence of a polar solvent and cyclopentadiene is effectively removed and recycled as a feedstock without being converted into its dimer, dicyclopentadiene. The isoprene recovered from the process described is more than 99.5% pure.

Abstract: Systems and processes for generating polyethylene are provided. A process includes performing a first reaction with methane and oxygen to produce a first product; performing a second reaction with the first product to produce a second product; separating components from the second product; returning ethane from the second product and performing a reaction simultaneous to the first reaction; performing a third reaction to produce a third product including polyethylene and vented methane; and returning the vented methane to a feed to the first reaction.

Abstract: The invention relates to a reactor comprising a plasma source and a catalyst comprising a mesoporous support. The invention also relates to a process comprising feeding methane to said reactor in order to obtain one or more of ethene, hydrogen and carbon as well as downstream products derived from ethene thus obtained. The invention relates to a reactor comprising as reactor parts: a. a housing and in said housing; b. a plasma source; and c. a catalyst, wherein said catalyst comprises as catalyst parts: i) a mesoporous support; ii) a metal selected from the group Pd, Ni, Ag or at least two thereof, wherein the metal is carried by said mesoporous support; wherein at least a part of said plasma source is located in said housing upstream of said catalyst.

Abstract: Co-extraction techniques for separating and purifying butadiene and isoprene from a C4 hydrocarbon mixture including butadiene and a C5 hydrocarbon mixture including isoprene are provided. In an exemplary embodiment, a system includes a dimerization heat exchanger, a C5 purification column; an extraction zone including a mainwasher column, a rectifier column and an afterwasher column; a distillation zone; a degassing zone; and an isoprene finishing column. The system can further include a C5 washer column, an absorption column, and a distillation column.

Abstract: Systems and processes for generating polyethylene are provided. A process includes performing a first reaction with methane and oxygen to produce a first product; performing a second reaction with the first product to produce a second product; separating components from the second product; returning ethane from the second product and performing a reaction simultaneous to the first reaction; performing a third reaction to produce a third product including polyethylene and vented methane; and returning the vented methane to a feed to the first reaction.

Abstract: A distillation system and process for separating a multi-component feed mixture in a distillation system comprising a first distillation column having a first fired reboiler, and at least a second distillation column having a second heat-exchange reboiler, comprising the steps of a) introducing the feed mixture to the first column, and separating into at least a first top and a first bottom product; b) taking part of the first bottom product for providing heat to the second reboiler as a utility stream; and c) feeding part of said utility stream after heat-exchange as main feed to the second column for further separation. This process allows significant energy savings, by reduction of the amount of external heat required for the fired reboiler and omission of a conventionally used heat-exchanger.