The present disclosure provides an apparatus for preparing oligomer including: a reactor; a gas-liquid separator; a solvent transfer line; a second transfer line; a first spray nozzle unit; and a second spray nozzle unit. The apparatus is capable of improving stability of the entire process by including a first spray nozzle unit and a second spray nozzle unit in a reactor and thus preventing by-products containing polymer substances such as C20+ from being entrained with a desired product during a reaction.

The present invention provides a process for recovering glycol from a process stream comprising glycol, water, dissolved salts, and hydrocarbons. The process comprises subjecting the process stream to a salt-enrichment process to obtain a salt-enriched stream having a salt concentration higher than salt concentration of the process stream, and a salt-reduced stream; subjecting the salt-enriched stream to a glycol reclaiming process to separate the salts and at least a portion of the hydrocarbons from the salt enriched stream to obtain a substantially salt-free water-glycol stream; and blending the salt reduced stream from the salt-enrichment process with the substantially salt-free stream to produce a reclaimed water-glycol stream

The present invention provides a process for recovering glycol from a process stream comprising glycol, water, dissolved salts, and hydrocarbons. The process comprises subjecting the process stream to a salt-enrichment process to obtain a salt-enriched stream having a salt concentration higher than salt concentration of the process stream, and a salt-reduced stream; subjecting the salt-enriched stream to a glycol reclaiming process to separate the salts and at least a portion of the hydrocarbons from the salt enriched stream to obtain a substantially salt-free water-glycol stream; and blending the salt reduced stream from the salt-enrichment process with the substantially salt-free stream to produce a reclaimed water-glycol stream

A processing facility is provided that includes a feedstock separation system configured to separate a feed stream into a lights stream and a heavies stream, a hydrogen production system configured to produce hydrogen and carbon dioxide from the lights stream, and a carbon dioxide conversion system configured to produce synthetic hydrocarbons or the carbon dioxide. The processing facility also includes a hydroprocessing system configured to process the heavies stream, and a hydroprocessor separation system configured to separate a hydroprocessing system effluent into a separator tops stream and a separator bottoms stream, wherein the separator bottoms stream is fed to the hydrogen production system.

A processing facility is provided that includes a feedstock separation system configured to separate a feed stream into a lights stream and a heavies stream, a hydrogen production system configured to produce hydrogen and carbon dioxide from the lights stream, and a carbon dioxide conversion system configured to produce synthetic hydrocarbons or the carbon dioxide. The processing facility also includes a hydroprocessing system configured to process the heavies stream, and a hydroprocessor separation system configured to separate a hydroprocessing system effluent into a separator tops stream and a separator bottoms stream, wherein the separator bottoms stream is fed to the hydrogen production system.

A hydrocracking process is disclosed. The hydrocracking process comprises hydrocracking a hydrocarbon feed stream in a hydrocracking reactor in the presence of a hydrogen stream and a hydrocracking catalyst to produce a hydrocracked effluent stream. The hydrocracked effluent stream is separated in a separator to provide a vapor hydrocracked stream and a liquid hydrocracked stream. The liquid hydrocracked stream is fractionated to provide a naphtha stream, a kerosene stream having a T90 temperature of about 204° C. (399° F.) to about 238° C. (460° F.), a diesel stream having a T90 temperature of about 360° C. (680° F.) to about 383° C. (721° F.) and an unconverted oil stream. The kerosene stream, the unconverted oil stream, and a portion of the diesel stream is recycled to the hydrocracking reactor for hydrocracking.

A hydrocracking process is disclosed. The hydrocracking process comprises hydrocracking a hydrocarbon feed stream in a hydrocracking reactor in the presence of a hydrogen stream and a hydrocracking catalyst to produce a hydrocracked effluent stream. The hydrocracked effluent stream is separated in a separator to provide a vapor hydrocracked stream and a liquid hydrocracked stream. The liquid hydrocracked stream is fractionated to provide a naphtha stream, a kerosene stream having a T90 temperature of about 204° C. (399° F.) to about 238° C. (460° F.), a diesel stream having a T90 temperature of about 360° C. (680° F.) to about 383° C. (721° F.) and an unconverted oil stream. The kerosene stream, the unconverted oil stream, and a portion of the diesel stream is recycled to the hydrocracking reactor for hydrocracking.

Provided are a method and device for preparing adiponitrile. The method of the present disclosure comprises the steps of a first hydrocyanation reaction, an isomerization reaction and a second hydrocyanation reaction, wherein online Raman spectroscopy is used for detecting the content of a specific component in the system; and the reaction conditions are regulated based on the detection results, so as to achieve precise control of the materials in each step of the reaction system. The method of the present disclosure can reduce an amount of butadiene, thereby reducing the subsequent energy consumption needed for recycling butadiene and equipment investment after reaction; by monitoring the content of hydrocyanic acid in real time, the residue of hydrocyanic acid is reduced to a lower level, and the operation safety and the stability of a catalyst during reaction are improved; and the loss of the catalyst is reduced.

Disclosed herein is a system for solution polymerization comprising a reactor system that is operative to receive a monomer and to react the monomer to form a polymer; a plurality of devolatilization vessels located downstream of the reactor system, where each devolatilization vessel operates at a lower pressure than the preceding devolatilization vessel; and a heat exchanger disposed between two devolatilization vessels and in fluid communication with them, where the heat exchanger has an inlet port temperature of 100° C. to 230° C., an outlet port temperature of 200° C. to 300° C., an inlet port pressure of 35 to 250 kgf/cm.sup.2 and an outlet port pressure of 20 to 200 kgf/cm.sup.2; and wherein the polymer solution remains in a single phase during its residence in the heat exchanger.

Disclosed is a purified dialkyl furan dicarboxylate (DAFD) vapor composition containing at least 99.5 wt. % DAFD; 5-(alkoxycarbonyl) furan-2-carboxylic acid (ACFC) that, if present, is present in an amount of not more than 1000 ppm, alkyl-5-formylfuran-2-carboxylate (AFFC) that, if present, is present in an amount of not more than 1000 ppm, 5-(dialkoxymethyl)furan-2-carboxylic acid (DAFCA) that if present, is present in an amount of not more than 1000 ppm, and alkyl 5-(dialkoxymethyl)furan-2-carboxylate (ADAFC) that if present, is present in an amount of not more than 1000 ppm, in each case based on the weight of the DAFD vapor composition.