Methods and systems to produce needle coke from aromatic recovery complex bottoms

Patent metadata

Field	Value
Publication number	US-11359148-B2
Application number	US-201916575148-A
Country	US
Kind code	B2
Filing date	Sep 18, 2019
Priority date	Sep 18, 2019
Publication date	Jun 14, 2022
Grant date	Jun 14, 2022

Abstract

Provided here are systems and methods of production of needle coke by processing an aromatic rejects stream containing long chain alkyl monoaromatics and bridged diaromatics through a delayed coking process. Various other embodiments may be disclosed and claimed.

First claim

What is claimed is:

1. A process for production of a needle coke product, the process comprising the steps of:
supplying a feed stream containing one or more of heavy alkyl aromatic compounds and alkyl-bridged non-condensed alkyl multi-aromatic compounds from an aromatic complex to a heating unit to produce a heated aromatic stream, wherein the heated aromatic stream contains between about 0 to about 200 ppmw sulfur;
supplying the heated aromatic stream to a coking unit with one coking drum under coking conditions to produce a coker vapor, a liquid product stream, and a petroleum coke product; and
removing the petroleum coke product from the one coking drum and supplying the petroleum coke product to a calcination unit to produce a needle coke product.

2. The process of claim 1 , wherein the feed stream is derived from a xylene rerun column of an aromatic recovery process.

3. The process of claim 2 , wherein the feed stream contains C 9+ compounds and is supplied from a fractionator adapted to fractionate a stream from the xylene rerun column to the feed stream.

4. The process of claim 1 , wherein the one or more of heavy alkyl aromatic compounds and alkyl-bridged non-condensed alkyl multi-aromatic compounds are C 11+ compounds.

5. The process of claim 1 , wherein the coking conditions include a temperature ranging from about 440° C. to about 530° C.

6. The process of claim 1 , wherein the coking conditions include a pressure ranging from about 1 bar to about 70 bars.

7. The process of claim 1 , further comprising the steps of:
removing the coker vapor and the liquid product stream from the coking unit; and
supplying water to the coking unit to quench a portion of the petroleum coke product before removing the petroleum coke product from the coking unit.

8. A process for production of a needle coke product, the process comprising the steps of:
supplying a feed stream containing one or more of heavy alkyl aromatic compounds and alkyl-bridged non-condensed alkyl multi-aromatic compounds from an aromatic complex to a hydrodearylation reactor to react in presence of a catalyst and hydrogen under specific reaction conditions to yield a first product stream containing hydrogen, C 1 to C 4 gases, benzene, toluene, xylenes, and C 9+ compounds;
supplying the first product stream to a separation unit to produce a hydrodearylated stream containing C 9+ compounds and a second product stream containing hydrogen, C 1 to C 4 gases, benzene, toluene, and xylenes;
supplying the hydrodearylated stream containing C 9+ compounds to a heating unit to produce a heated aromatic stream, wherein the heated aromatic stream contains between about 0 to about 200 ppmw sulfur;
supplying the heated aromatic stream to a coking unit with one coking drum under coking conditions to produce a coker vapor, a liquid product stream, and a petroleum coke product; and
removing the petroleum coke product from the one coking drum and supplying the petroleum coke product to a calcination unit to produce a needle coke product.

9. The process of claim 8 , wherein the coking conditions include a temperature ranging from about 440° C. to about 530° C.

10. The process of claim 8 , wherein the coking conditions include a pressure ranging from about 1 bar to about 70 bars.

11. The process of claim 8 , further comprising the steps of:
removing the coker vapor and the liquid product stream from the coking unit; and
supplying water to the coking unit to quench a portion of the petroleum coke product before removing the petroleum coke product from the coking unit.

12. The process of claim 8 , wherein the feed stream is from a xylene rerun column of an aromatic recovery process.

13. The process of claim 8 , wherein conditions in the hydrodearylation reactor include an operating temperature in the range of about 200° C. to about 450° C.

14. The process of claim 8 , wherein conditions in the hydrodearylation reactor include an operating pressure in the range of about 5 bar gauge to about 80 bar gauge.

15. The process of claim 8 , wherein a volumetric ratio of hydrogen to hydrocarbon components in the hydrodearylation reactor ranges from 50 to 2500 Nm 3 /m 3 .

Assignees

• Saudi Arabian Oil Co

Inventors

• Koseoglu Omer Refa
• Hodgkins Robert Peter

Classifications

• C10B55/00

  Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material (cracking oils C10G) · CPC title

• C10B57/08

  Non-mechanical pretreatment of the charge (C10L9/00 takes precedence), {e.g. desulfurization} · CPC title

• C10G69/06

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

• C10B57/04 Primary

  using charges of special composition · CPC title

• C10G2300/1096

  Aromatics or polyaromatics · CPC title