Process for producing BTX from a mixed hydrocarbon source using catalytic cracking

Patent metadata

Field	Value
Publication number	US-10358612-B2
Application number	US-201415120538-A
Country	US
Kind code	B2
Filing date	Dec 10, 2014
Priority date	Feb 25, 2014
Publication date	Jul 23, 2019
Grant date	Jul 23, 2019

Abstract

The present invention relates to a process for producing BTX comprising catalytic cracking, aromatic ring opening and BTX recovery. Furthermore, the present invention relates to a process installation to convert a hydrocarbon feedstream into BTX comprising a catalytic cracking unit, an aromatic ring opening unit and a BTX recovery unit.

First claim

The invention claimed is:

1. A process for producing BTX comprising:
(a) subjecting a hydrocarbon feedstream to catalytic cracking to produce catalytic cracking gasoline and cycle oil;
(b) subjecting cycle oil in the presence of hydrogen and an aromatic ring opening catalyst to aromatic ring opening to produce BTX; and
(c) recovering BTX from catalytic cracking gasoline.

2. A process for producing BTX comprising:
(a) subjecting a hydrocarbon feedstream to catalytic cracking to produce catalytic cracking gasoline and cycle oil;
(b) subjecting cycle oil to aromatic ring opening to produce BTX; and
(c) recovering BTX from catalytic cracking gasoline, wherein the aromatic ring opening further produces light-distillate and wherein the BTX is recovered from said light-distillate.

3. A process for producing BTX comprising:
(a) subjecting a hydrocarbon feedstream to catalytic cracking to produce catalytic cracking gasoline and cycle oil;
(b) subjecting cycle oil to aromatic ring opening to produce BTX; and
(c) recovering BTX from catalytic cracking gasoline, wherein the BTX is recovered from the catalytic cracking gasoline and/or from the light-distillate by subjecting said catalytic cracking gasoline and/or light-distillate to hydrocracking.

4. The process according to claim 1 , wherein the aromatic ring opening and the hydrocracking further produce LPG and wherein said LPG is subjected to aromatization to produce BTX.

5. The process according to claim 1 , wherein the catalytic cracking further produces LPG and wherein said LPG produced by catalytic cracking is subjected to aromatization to produce BTX.

6. The process according to claim 5 , wherein propylene and/or butylenes are separated from the LPG produced by catalytic cracking before subjecting to aromatization.

7. The process according to claim 1 , wherein the catalytic cracking is fluid catalytic cracking comprising contacting the feedstream with an FCC catalyst under FCC conditions, wherein
the FCC catalyst comprises zeolite and wherein
the FCC conditions comprise a temperature of 425-730° C. and a pressure of 10-800 kPa gauge.

8. The process according to claim 1 , wherein the catalytic cracking is high-severity FCC, comprising a temperature of 540-730° C. and a pressure of 10-800 kPa gauge.

9. The process according to claim 1 , wherein said hydrocracking comprises contacting the catalytic cracking gasoline and the light-distillate in the presence of hydrogen with a hydrocracking catalyst under hydrocracking conditions, wherein
the hydrocracking catalyst comprises 0.1-1 wt-% hydrogenation metal in relation to the total catalyst weight and a zeolite having a pore size of 5-8 Å and a silica (SiO 2 ) to alumina (Al 2 O 3 ) molar ratio of 5-200 and wherein
the hydrocracking conditions comprise a temperature of 400-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity (WHSV) of 0.1-20 h −1 .

10. The process according to claim 1 , wherein said aromatic ring opening comprises contacting the cycle oil in the presence of hydrogen with an aromatic ring opening catalyst under aromatic ring opening conditions, wherein
the aromatic ring opening catalyst comprises a transition metal or metal sulphide component and a support, and wherein
the aromatic ring opening conditions comprise a temperature of 100-600° C., a pressure of 1-12 MPa.

11. The process according to claim 10 , wherein the aromatic ring opening catalyst comprises an aromatic hydrogenation catalyst comprising one or more elements selected from the group consisting of Ni, W and Mo on a refractory support; and a ring cleavage catalyst comprising a transition metal or metal sulphide component and a support and wherein the conditions for aromatic hydrogenation comprise a temperature of 100-500° C., a pressure of 2-10 MPa and the presence of 1-30 wt-% of hydrogen in relation to the hydrocarbon feedstock and wherein the ring cleavage comprises a temperature of 200-600° C., a pressure of 1-12 MPa and the presence of 1-20 wt-% of hydrogen in relation to the hydrocarbon feedstock.

12. The process according to claim 4 , wherein the aromatization comprises contacting the LPG with an aromatization catalyst under aromatization conditions, wherein
the aromatization catalyst comprises a zeolite selected from the group consisting of ZSM-5 and zeolite L, optionally further comprising one or more elements selected from the group consisting of Ga, Zn, Ge and Pt and wherein
the aromatization conditions comprise a temperature of 400-600° C., a pressure of 100-1000 kPa gauge and a Weight Hourly Space Velocity (WHSV) of 0.1-20 h −1 .

13. The process according to claim 4 , wherein the LPG produced by hydrocracking and aromatic ring opening is subjected to a first aromatization that is optimized towards aromatization of paraffinic hydrocarbons, wherein said first aromatization comprises the aromatization conditions comprising a temperature of 400-600° C., a pressure of 100-1000 kPa gauge and a Weight Hourly Space Velocity (WHSV) of 0.1-7 h −1 ; and/or wherein
the LPG produced by catalytic cracking are subjected to a second aromatization that is optimized towards aromatization of olefinic hydrocarbons, wherein said second aromatization comprises the aromatization conditions comprising a temperature of 400-600° C., a pressure of 100-1000 kPa gauge and a Weight Hourly Space Velocity (WHSV) of 1-20 h −1 .

14. The process according to claim 1 , wherein one or more of the group consisting of the aromatic ring opening, the hydrocracking and the aromatization further produce methane and wherein said methane is used as fuel gas to provide process heat.

15. The process according to claim 1 , wherein the hydrocarbon feedstream comprises one or more selected from the group consisting of naphtha, kerosene, gasoil and resid.

16. The process according to claim 4 , wherein the aromatization further produces hydrogen and wherein said hydrogen is used in the hydrocracking and/or the aromatic ring opening.

17. The process according to claim 10 , wherein the support comprises one or more elements selected from the group consisting of Pd, Rh, Ru, Ir, Os, Cu, Co, Ni, Pt, Fe, Zn, Ga, In, Mo, W and V in metallic or metal sulphide form supported on an acidic solid.

18. The process according to claim 17 , wherein the support is selected from the group consisting of alumina, silica, alumina-silica and zeolites.

Assignees

• Saudi Basic Ind Corp
• Sabic Global Technologies Bv
• Pelaez Raul Velasco

Inventors

• Pelaez Raul Velasco

Classifications

• C10G2400/30

  Aromatics · CPC title

• C10G2300/1059

  Gasoil having a boiling range of about 330 - 427 °C · CPC title

• C10G2300/1044

  Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C · CPC title

• C10G69/04 Primary

  including at least one step of catalytic cracking in the absence of hydrogen · CPC title

• C10G69/02 Primary

  plural serial stages only · CPC title