Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include light products and naphtha from hydroprocessing zones within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feeds to the gas oil steam cracker include hydrotreated gas oil range intermediates from the vacuum gas oil hydroprocessing zone. Furthermore, vacuum residue is processed in a solvent deasphalting unit to produce deasphalted oil as additional feed to the gas oil hydroprocessing zone.

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include light products and naphtha from hydroprocessing zones within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feeds to the gas oil steam cracker include hydrotreated gas oil range intermediates from the vacuum gas oil hydroprocessing zone. Furthermore, vacuum residue is processed in a solvent deasphalting unit to produce deasphalted oil as additional feed to the gas oil hydroprocessing zone.

Process scheme configurations are disclosed that enable conversion of crude oil feeds with several processing units in an integrated manner into petrochemicals. The designs utilize minimum capital expenditures to prepare suitable feedstocks for the steam cracker complex. The integrated process for converting crude oil to petrochemical products including olefins and aromatics, and fuel products, includes mixed feed steam cracking and gas oil steam cracking. Feeds to the mixed feed steam cracker include light products and naphtha from hydroprocessing zones within the battery limits, recycle streams from the C3 and C4 olefins recovery steps, and raffinate from a pyrolysis gasoline aromatics extraction zone within the battery limits. Feeds to the gas oil steam cracker include hydrotreated gas oil range intermediates from the vacuum gas oil hydroprocessing zone. Furthermore, vacuum residue is processed in a solvent deasphalting unit to produce deasphalted oil as additional feed to the gas oil hydroprocessing zone.

The present disclosure relates to a method of refining waste plastic pyrolysis oil comprising: mixing waste plastic pyrolysis oil and waste tire pyrolysis oil to produce a mixed oil; hydrotreating the mixed oil with a reaction gas comprising hydrogen gas (H.sub.2) in the presence of a molybdenum-based hydrotreating catalyst; and removing a by-product of the hydrotreating from a product of step (S2) to obtain refined oil. The method of refining waste plastic pyrolysis oil disclosed herein may produce refined oil having a significantly low content of impurities such as chlorine, nitrogen, oxygen, and/or metals, and reduces the environmental load due to waste tires by diverting waste tire pyrolysis oil to supply a continuous sulfur source, such that the refining device may operate continuously for a long period of time.

The present disclosure relates to a method of refining waste plastic pyrolysis oil comprising: mixing waste plastic pyrolysis oil and waste tire pyrolysis oil to produce a mixed oil; hydrotreating the mixed oil with a reaction gas comprising hydrogen gas (H.sub.2) in the presence of a molybdenum-based hydrotreating catalyst; and removing a by-product of the hydrotreating from a product of step (S2) to obtain refined oil. The method of refining waste plastic pyrolysis oil disclosed herein may produce refined oil having a significantly low content of impurities such as chlorine, nitrogen, oxygen, and/or metals, and reduces the environmental load due to waste tires by diverting waste tire pyrolysis oil to supply a continuous sulfur source, such that the refining device may operate continuously for a long period of time.

One or more liquid organic hydrogen carriers may be processed by a method that includes passing one or more hydrogen-diminished liquid organic hydrogen carriers and hydrogen into a hydrogenation reactor to form a hydrogenation reactor effluent. The hydrogenation reactor effluent may include one or more hydrogen-rich liquid organic hydrogen carriers and unreacted hydrogen. the method may further include passing the hydrogenation reactor effluent from the hydrogenation reactor to a separation unit and separating at least the one or more hydrogen-rich liquid organic hydrogen carriers from the unreacted hydrogen in the separation unit. The method may further include passing at least a naphtha feed and the unreacted hydrogen to a naphtha hydrotreater to produce a hydrotreater effluent that includes a hydrotreated naphtha.