Method for producing light aromatic

Patent metadata

Field	Value
Publication number	US-12054680-B2
Application number	US-202017755033-A
Country	US
Kind code	B2
Filing date	Aug 4, 2020
Priority date	Oct 30, 2019
Publication date	Aug 6, 2024
Grant date	Aug 6, 2024

Abstract

A method for producing light aromatics, includes the steps of: i) contacting a feedstock comprising heavy aromatic(s) with a catalyst in a fluidized reactor for aromatics lightening reaction in the presence of hydrogen to obtain a product rich in C6-C8 light aromatic(s) and a spent catalyst, wherein the heavy aromatic is one or more selected from C9+ aromatics; ii) separating the resulted product rich in C6-C8 light aromatic(s) to obtain hydrogen, a non-aromatic component, C6-C8 light aromatic(s) and a C9+ aromatic component; and iii) recycling at least a part of the C9+ aromatic component to the fluidized reactor. The method has strong adaptability to feedstocks and high flexibility in operation and allows a long-period stable operation. The method can produce high-value light aromatics from heavy aromatics that are difficult to be treated and utilized.

First claim

The invention claimed is:

1. A method for producing light aromatics, comprising the steps of:
i) contacting a feedstock with a catalyst in a fluidized reactor for aromatics lightening reaction in the presence of hydrogen to obtain a product rich in C6-C8 light aromatics and a spent catalyst, wherein the feedstock comprises heavy aromatics that is one or more selected from C9+ aromatics;
ii) separating the product rich in C6-C8 light aromatics to obtain hydrogen, a non-aromatic component, C6-C8 light aromatics and a C9+ aromatic component; and
iii) recycling at least a part of the C9+ aromatic component to the fluidized reactor,
wherein:
the reaction conditions of step i) include: a temperature of about 250-750° C., a pressure of about 0-6 MPa, a weight hourly space velocity of about 0.1-120 h −1 or a reaction time of about 0.1-40 seconds, and a hydrogen/hydrocarbon molar ratio of about 1-15, wherein the pressure is a gauge pressure,
the catalyst in step i) comprises a carrier and an active metal component supported on the carrier in an amount of about 0.01-50 wt %, based on the total weight of the catalyst,
wherein the carrier comprises from about 1 wt % to about 80 wt % of zeolite, from about 5 wt % to about 99 wt % of inorganic oxide, and from about 0 wt % to about 70 wt % of clay, based on the total weight of the carrier, wherein the zeolite comprises a mesoporous zeolite, a macroporous zeolite, or a combination thereof; the inorganic oxide is one or more selected from silica, alumina, zirconia, titania, and amorphous silica-alumina; the clay is one or more selected from kaolin, montmorillonite, diatomite, attapulgite, sepiolite, halloysite, hydrotalcite, bentonite, and rectorite,
the active metal component is one or more selected from rare earth metals and transition metals,
wherein the separation of step ii) further comprises the steps of:
subjecting the product rich in C6-C8 light aromatics to gas-liquid separation to obtain hydrogen and a liquid product;
subjecting the liquid product to aromatics extraction to obtain a non-aromatic component and an aromatic component; and
subjecting the aromatic component to a first fractionation to obtain C6-C8 light aromatics and a C9+ aromatic component, or subjecting the aromatic component to a second fractionation to obtain C6-C8 light aromatics, C9 aromatics, and a C10+ aromatic component.

2. The method according to claim 1 , wherein the reaction conditions of step i) include: a temperature of about 320-600° C., a pressure of about 0-4.5 MPa, a weight hourly space velocity of about 1-80 h −1 or a reaction time of about 0.5-30 seconds, and a hydrogen/hydrocarbon molar ratio of about 2-10.

3. The method according to claim 1 , wherein after said step ii), the method further comprises one or more steps selected from:
subjecting the C6-C8 light aromatics to a third fractionation to obtain benzene, toluene and xylene;
mixing the toluene and the C9 aromatics to obtain a mixed recycle feed, and recycling the mixed recycle feed to the fluidized reactor; and
mixing the C10+ aromatic component with the feedstock and recycling the resulting mixture to the fluidized reactor.

4. The method according to claim 3 , wherein the mixed recycle feed is recycled to the fluidized reactor at a position downstream of the position at which the resulting mixture containing the C10+ aromatic component is recycled, along the flow direction of the feedstock within the fluidized reactor.

5. The method according to claim 1 , further comprising the step of:
regenerating the spent catalyst in a fluidized bed regenerator and recycling the regenerated catalyst to the fluidized reactor.

6. The method according to claim 5 , wherein the fluidized bed regenerator comprises a lock hopper, and the regeneration is carried out by:
sending the spent catalyst to the fluidized bed regenerator for regeneration through the lock hopper, and recycling the regenerated catalyst to the fluidized reactor through the lock hopper.

7. The method according to claim 6 , further comprising the step of depressurizing the spent catalyst in the lock hopper and the step of pressurizing the regenerated catalyst in the lock hopper.

8. The method according to claim 6 , wherein the fluidized bed regenerator further comprises a reactor receiver, a regenerator receiver, a regenerator feed tank, and optionally a reducer, and the regeneration is carried out by:
sending the spent catalyst from the fluidized reactor to the reactor receiver, then to the regenerator feed tank through the lock hopper, and then from the regenerator feed tank to the fluidized bed regenerator;
subjecting the spent catalyst to regeneration by coke-burning in the regenerator under an oxygen-containing atmosphere to obtain the regenerated catalyst; and
recycling the regenerated catalyst from the fluidized bed regenerator, to the fluidized reactor for reuse directly through the regenerator receiver, or to the fluidized reactor for reuse after being reduced in a reducer.

9. The method according to claim 1 , wherein the feedstock has an initial boiling point of about 120° C. to about 150° C. and a final boiling point of about 200° C. to about 250° C.

10. The method according to claim 1 , wherein the feedstock is at least one selected from heavy aromatics derived from steam cracking gasoline, heavy aromatics derived from deep catalytic cracking gasoline, heavy aromatics derived from catalytic cracking gasoline, and heavy aromatics derived from catalytic reforming and C9+ heavy aromatics from a bottom of xylene column in aromatics complex plant.

11. The method according to claim 1 , wherein the fluidized reactor is selected from a conveying bed reactor, a dense-phase fluidized bed reactor, a composite reactor composed of a conveying bed reactor and a dense-phase fluidized bed reactor, a composite reactor composed of two or more conveying bed reactors, and a composite reactor composed of two or more dense-phase fluidized bed reactors.

12. The method according to claim 11 , wherein the conveying bed reactor is a riser reactor; and the dense-phase fluidized bed reactor is a bubbling fluidized bed reactor or a turbulent fluidized bed reactor.

13. The method according to claim 1 , wherein the mesoporous zeolite is one or more selected from ZSM zeolites and ZRP zeolites, and the macroporous zeolite is one or more selected from ß zeolites, REY zeolites, REHY zeolites, ultrastable Y zeolites, and high silica Y zeolites.

14. The method according to claim 1 , wherein the mesoporous zeolite is present in an amount of from about 0 wt % to about 100 wt %, and the macroporous zeolite is present in an amount of from about 0 wt % to about 100 wt %, based on the total weight of the zeolite.

15. The method according to claim 14 , wherein the mesoporous zeolite is present in an amount of from about 50 wt % to about 100 wt %.

16. The method according to claim 14 , wherein the mesoporous zeolite is present in an amount of from about 70 wt % to about 90 wt %.

17. The method according to claim 14 , wherein the macroporous zeolite is present in an amount of from about 0 wt % to about 50 wt %.

18. The method according to claim 14 , wherein the macroporous zeolite is present in an amount of from about 10 wt % to about 30 wt %.

19. The method according to claim 1 , wherein the reaction conditions of step i) include: a temperature of about 360-550° C., a pressure of about 1-3 MPa, a weight hourly space velocity of about 1.5-50 h −1 or a reaction time of about 1-15 seconds, and a hydrogen/hydrocarbon mo

Assignees

• China Petroleum & Chem Corp
• Sinopec Res Inst Petroleum

Inventors

• Wang Di
• Wei Xiaoli
• Gong Jianhong
• Yu Jingchuan
• Zhang Jiushun

Classifications

• C10G2400/30

  Aromatics · CPC title

• C10G2300/708

  Coking aspect, coke content and composition of deposits · CPC title

• C10G2300/4018

  Spatial velocity, e.g. LHSV, WHSV · CPC title

• C10G2300/4012

  Pressure · CPC title

• C10G2300/4006

  Temperature · CPC title