Systems and processes for producing ethylene from naphtha and butanes
A process for upgrading a hydrocarbon feed includes contacting the hydrocarbon feed with hydrogen in the presence of a ring opening catalyst in a naphthene conversion unit, the contacting causing naphthenes in the hydrocarbon feed to react to produce a converted effluent comprising isoparaffins and normal paraffins. The process includes separating the converted effluent in a paraffin separation system to produce an isoparaffin-rich stream and an n-paraffin-rich stream. The process includes contacting the isoparaffin-rich stream with hydrogen in the presence of an isomerization catalyst in a reverse isomerization unit, the contacting causing isomerization to produce an isomerate comprising an equilibrium mixture of normal paraffins and isoparaffins. The process include separating the isomerate in the paraffin separation system to produce the isoparaffin-rich stream and the n-paraffin-rich stream, and passing the n-paraffin-rich stream to a steam cracker to produce a cracker effluent comprising olefins.
1. A process for upgrading a hydrocarbon feed, the process comprising:
passing the hydrocarbon feed to a naphthene conversion unit, where the hydrocarbon feed comprises naphthenes;
contacting the hydrocarbon feed with hydrogen in the presence of a ring opening catalyst in the naphthene conversion unit, where the contacting causes at least a portion of the naphthenes in the hydrocarbon feed to react to produce a converted effluent comprising at least isoparaffins and normal paraffins;
passing at least a portion of the converted effluent to a paraffin separation system that separates the at least a portion of the converted effluent to produce at least one isoparaffin-rich stream and at least one n-paraffin-rich stream;
passing a butane-containing stream to the paraffin separation system that separates the butane-containing stream into the at least one isoparaffin-rich stream and the at least one n-paraffin-rich stream, wherein the at least one isoparaffin-rich stream comprises isobutane from the butane-containing stream, and the at least one n-paraffin-rich stream may comprise normal butane from the butane-containing stream;
passing the at least one n-paraffin-rich stream to a steam cracker to produce a cracker effluent comprising at least one product.
2. The process of claim 1 , further comprising passing the at least one isoparaffin-rich stream to a reverse isomerization unit.
3. The process of claim 2 , wherein the reverse isomerization unit operates in a liquid phase, a vapor phase, or both.
4. The process of claim 2 , further comprising contacting the at least one isoparaffin-rich stream with hydrogen in the presence of an isomerization catalyst in the reverse isomerization unit, where the contacting in the reverse isomerization unit causes at least a portion of the isoparaffins in the at least one isoparaffin-rich stream to undergo isomerization to produce an isomerate comprising a mixture of normal paraffins and isoparaffins.
5. The process of claim 4 , further comprising passing at least a portion of the isomerate to the paraffin separation system that separates the at least a portion of the isomerate to produce the at least one isoparaffin-rich stream and the at least one n-paraffin-rich stream.
6. The process of claim 4 , further comprising:
passing the isomerate to an isomerate separator that separates the isomerate to produce at least an isomerate light gas stream, a C3-C4 isomerate effluent, and a C5+ isomerate effluent; and
passing the C5+ isomerate effluent to the paraffin separation system.
7. The process of claim 1 , wherein the naphthene conversion unit comprises one or more fixed bed reactors, ebullated bed reactors, moving bed reactors, or combinations thereof.
8. The process of claim 1 , wherein the ring opening catalyst comprises one or more transition metals from groups 8-10 of the IUPAC periodic table supported on a catalyst support comprising alumina, silica, titania, or combinations thereof.
9. The process of claim 8 , where the one or more transition metals may be selected from the group consisting of Ir, Pt, Pd, Rh, Ru, and combinations of these metals.
10. The process of claim 8 , wherein the catalyst support may be non-acidic or mildly acidic.
11. The process of claim 1 , wherein a conversion of naphthenes in the naphthene conversion unit is greater than or equal to 95 wt. % based on a total weight of naphthenes in the hydrocarbon feed.
12. The process of claim 1 , further comprising conditioning the hydrocarbon feed in one or more guard beds prior to passing the hydrocarbon feed to the naphthene conversion unit.
13. The process of claim 12 , wherein:
the guard bed comprises a desulfurization catalyst; and
conditioning the hydrocarbon feed in the one or more guard beds comprises contacting the hydrocarbon feed with the desulfurization catalyst, wherein the contacting the hydrocarbon feed with the desulfurization catalyst reduces a concentration of sulfur in the hydrocarbon feed to produce a conditioned hydrocarbon feed.
14. The process of claim 1 , wherein the naphthene conversion unit is a vapor phase reaction system or a two-phase reaction system.
15. The process of claim 1 , where the hydrocarbon feed comprises a naphtha feed comprising a straight run naphtha, a hydrotreated naphtha, or combinations of these.
16. The process of claim 1 , where the hydrocarbon feed comprises an average carbon number of from 4 to 12, a boiling point temperature range of from −5° C. to 220° C., or both.
17. The process of claim 1 , where the hydrocarbon feed comprises from 40 wt. % to 60 wt. % naphthenes based on a total weight of the hydrocarbon feed, a molar ratio of iso-paraffins to normal paraffins of from 1:2 to 4:1, or both.
18. The process of claim 1 , comprising contacting the hydrocarbon feed with the hydrogen in the presence of the ring opening catalyst in the naphthene conversion unit at one or more of the following reaction conditions:
a naphthene conversion temperature of from 150° C. to 400° C.;
a naphthene conversion pressure of from 1000 kPa to 10,000 kPa (10 bars to 100 bars);
a hydrogen partial pressure of from 1000 kPa to 6000 kPa;
a liquid hourly space velocity of from 0.2 hour −1 to 20 hour −1 ; or
combinations of these operating conditions.
19. The process of claim 1 , where the converted effluent comprises at least 75% paraffins, wherein the paraffins include normal paraffins, isoparaffins, or combinations thereof.
20. The process of claim 1 , further comprising:
passing the converted effluent to a converted effluent separation system that separates the converted effluent to produce at least a light naphtha and a heavy naphtha;
passing the heavy naphtha to the steam cracker; and
passing the light naphtha to the paraffin separation system.