Processes and systems for petrochemical production integrating fluid catalytic cracking and deep hydrogenation of fluid catalytic cracking reaction products

1. A process for petrochemical production comprising:

providing a feedstock selected from the group consisting of naphtha, diesel or heavy oils;

subjecting the feedstock to fluid catalytic cracking to produce at least light cycle oil;

subjecting all or a portion of the light cycle oil to hydrogenation to hydrogenate aromatics contained in the light cycle oil and produce hydrogenated middle distillates, wherein hydrogenation occurs in the presence of an effective quantity of a hydrogenation catalyst containing one or more active metal components selected from Pt, Pd, Re and a combination comprising at least two of Pt, Pd or Re, and the hydrogenation catalyst including a catalyst support comprising non-acidic amorphous alumina and about 0.1-15 wt % of a modified USY zeolite having one or more of Ti, Zr and/or Hf substituting aluminum atoms constituting the zeolite framework thereof; and

subjecting all or a portion of the hydrogenated middle distillates to thermal cracking in a steam cracking complex to obtain light olefins.

2. The process as in claim 1 , wherein

the feedstock is a heavy oil selected from the group consisting of atmospheric gas oil, heavy atmospheric gas oil, vacuum gas oil, atmospheric residue, deasphalted oil, demetallized oil, coker gas oil, gas oil obtained from a visbreaking process, and combinations comprising at least one of the foregoing heavy oils.

3. The process as in claim 1 , further comprising hydrotreating all or a portion of the light cycle oil to produce hydrotreated light cycle oil, and subjecting all or a portion of the hydrotreated light cycle oil to hydrogenation.

4. The process as in claim 1 , wherein

thermal cracking further produces pyrolysis gasoline, the process further comprising passing all or a portion of the pyrolysis gasoline to hydrotreating, separating all or a portion of the hydrotreated pyrolysis gasoline into a raffinate stream that is recycled to the steam cracking complex and an extract stream that is used for BTX recovery.

5. The process as in claim 4 , further wherein

fluid catalytic cracking produces FCC naphtha, and wherein all or a portion of the FCC naphtha is separated together with all or a portion of the hydrotreated pyrolysis gasoline.

6. The process as in claim 4 , further wherein

fluid catalytic cracking produces FCC naphtha, the process further comprising hydrotreating all or a portion of the FCC naphtha produced by fluid catalytic cracking, and wherein all or a portion of the hydrotreated FCC naphtha is separated together with all or a portion of the hydrotreated pyrolysis gasoline.

7. The process as in claim 1 , wherein

fluid catalytic cracking produces FCC naphtha, the process further comprising hydrotreating all or a portion of the FCC naphtha produced by fluid catalytic cracking, hydrogenating all or a portion of the FCC naphtha, and subjecting all or a portion of the hydrogenated products from hydrogenation of hydrotreated FCC naphtha to thermal cracking to obtain light olefins.

8. The process as in claim 7 , further comprising

the steam cracking complex comprises a common unit for cracking all or a portion of the hydrogenated products from hydrogenation of hydrotreated FCC naphtha and all or a portion of the hydrogenated middle distillates from hydrogenation.

9. The process as in claim 7 , wherein

the steam cracking complex comprises plural sections for cracking all or a portion of the hydrogenated products from hydrogenation of hydrotreated FCC naphtha and all or a portion of the hydrogenated middle distillates from hydrogenation separately based on boiling point characteristics.

10. The process as in claim 1 , wherein fluid catalytic cracking is with a riser reactor operating with:

a reaction temperature of from about 480-650° C.;

a reaction pressure of from about 1-20 barg;

a contact time (in the reactor, seconds) of from about 0.5-10; and

a catalyst-to-feed ratio of about 1:1 to 15:1.

11. The process as in claim 1 , wherein fluid catalytic cracking is with a downflow reactor operating with:

a reaction temperature of from about 550-650° C.;

a reaction pressure of from about 1-20 barg;

a contact time (in the reactor, seconds) of from about 0.1-30; and

a catalyst-to-feed ratio of about 1:1 to 40:1.

12. The process as in claim 1 , wherein

hydrogenation occurs at a hydrogen partial pressure of about 50-150 barg.

13. The process as in claim 1 , wherein

hydrogenation occurs at a reaction temperature of about 250-400° C.

14. The process as in claim 1 , wherein

hydrogenation occurs at a liquid hourly space velocity values, on a fresh feed basis relative to the hydrogenation catalyst, of about 0.1-5 h −1 .

15. The process as in claim 1 , wherein

hydrogenation occurs at a hydrogen to oil feed ratio of about 100-1500 SLt/Lt.

16. The process as in claim 1 , wherein hydrogenation occurs

at a hydrogen partial pressure of about 50-150 barg;

at a reaction temperature of about 250-400° C.;

at a liquid hourly space velocity values, on a fresh feed basis relative to the hydrogenation catalyst, of about 0.1-5.0 h −1 ; and

at a hydrogen to oil feed ratio of about 100-1500 SLt/Lt.

17. The process as in claim 1 , wherein the light cycle oil subjected to hydrogenation contain at least about 10 weight % aromatics, and wherein the hydrogenated middle distillates contain less than about 1 weight % aromatics.

18. The process as in claim 1 , wherein, prior to hydrogenation of all or a portion of the light cycle oil,

all or a portion of the light cycle oil is mixed with an excess of hydrogen gas in a mixing zone to produce a mixture of

hydrogen-enriched light cycle oil, and

undissolved hydrogen;

passing the mixture to a flashing zone wherein at least a portion of undissolved hydrogen is flashed, and obtaining a hydrogen-enriched light cycle oil stream; and

subjecting the hydrogen-enriched light cycle oil stream to hydrogenation.

19. A system for petrochemical production comprising:

a source of feedstock selected from the group consisting of naphtha, diesel or heavy oils;

a fluid catalytic cracking zone operable to produce at least light cycle oil from the feedstock;

a fixed-bed hydrogenation zone operable to produce hydrogenated middle distillates from all or a portion of the light cycle oil produced in the fluid catalytic cracking zone, the hydrogenation zone containing an effective quantity of a hydrogenation catalyst, the hydrogenation catalyst

containing one or more active metal components selected from Pt, Pd, Re and a combination comprising at least two of Pt, Pd or Re, and

including a catalyst support comprising non-acidic amorphous alumina and about 0.1-15 wt % of a modified USY zeolite having one or more of Ti, Zr and/or Hf substituting aluminum atoms constituting the zeolite framework thereof; and

a steam cracking complex operable to thermally crack all or a portion of the hydrogenated middle distillates for production of light olefins.