阅读说明：本技术 用于原油转化的系统和方法 (System and method for crude oil conversion ) 是由 埃萨姆·阿尔-萨伊德 奥马尔·瑞法·高斯奥格鲁 丁连辉 阿布德努尔·布兰 阿尔贝托·洛扎诺· 于 2018-04-20 设计创作，主要内容包括：根据本公开的一个实施例,可以通过一种方法由原油产生石化产品,所述方法包括将所述原油和氢气传递到加氢处理反应器,将加氢处理的油分离成较低沸点馏分和较高沸点馏分,将所述较低沸点馏分传递到蒸汽裂解器的热解段以产生包含烯烃、芳香烃或两者的热解流出物,将所述较高沸点馏分传递到气化炉,其中所述气化炉产生氢气,以及将由所述气化炉产生的所述氢气的至少一部分传递到所述加氢处理反应器。(According to one embodiment of the present disclosure, petrochemicals may be produced from crude oil by a method comprising passing the crude oil and hydrogen to a hydroprocessing reactor, separating hydroprocessed oil into a lower boiling fraction and a higher boiling fraction, passing the lower boiling fraction to a pyrolysis section of a steam cracker to produce a pyrolysis effluent comprising olefins, aromatic hydrocarbons, or both, passing the higher boiling fraction to a gasifier, wherein the gasifier produces hydrogen, and passing at least a portion of the hydrogen produced by the gasifier to the hydroprocessing reactor.)

1. A method for producing petrochemicals from crude oil, the method comprising:

Passing the crude oil and hydrogen into a hydroprocessing reactor, the hydroprocessing reactor comprising one or more hydroprocessing catalysts that produce a hydroprocessed oil;

Separating the hydrotreated oil into a lower boiling fraction and a higher boiling fraction;

Passing the lower boiling fraction to a pyrolysis section of a steam cracker to produce a pyrolysis effluent comprising olefins, aromatic hydrocarbons, or both;

Passing the higher boiling fraction to a gasifier, wherein the gasifier produces hydrogen; and

Passing at least a portion of the hydrogen produced by the gasifier to the hydrotreating reactor.

2. the method of claim 1, wherein the crude oil is combined with the hydrogen to form a mixed stream that is passed into the hydroprocessing reactor.

3. The process of any of the preceding claims, further comprising passing the hydrotreated oil to the steam cracker, the steam cracker comprising a convection section operated at a temperature of 700 ℃ to 900 ℃ to produce a heated hydrotreated oil.

4. The process of any of the preceding claims, further comprising passing the pyrolysis effluent to at least one separator, wherein the at least one separator converts the pyrolysis effluent into one or more product streams comprising the olefins, aromatic hydrocarbons, or both.

5. The method of any one of the preceding claims, wherein the hydrotreating reactor comprises one or more of a hydrodemetallization catalyst, a hydrocracking catalyst, a hydrodearomatization catalyst, a hydrodenitrogenation catalyst, or a hydrodesulfurization catalyst.

6. The method of claim 5, wherein the hydrotreating reactor comprises a hydrodemetallization catalyst disposed upstream of other hydrotreating catalysts.

7. The process of any of the preceding claims, wherein the pyrolysis effluent further comprises hydrogen, which is passed to the hydroprocessing reactor.

8. The process of any one of the preceding claims, wherein the pyrolysis effluent comprises aromatic hydrocarbons selected from one or more of benzene, toluene, or xylene.

9. The method of any one of the preceding claims, wherein the gasifier comprises a moving bed system, a fluidized bed system, an entrained flow system, or a combination thereof.

10. The process of any of the preceding claims, wherein the higher boiling fraction comprises solid matter.

11. The method of any one of the preceding claims, further comprising:

Passing the hydrogen produced in the separator to a hydrogen purification unit, wherein hydrogen purification produces a treated hydrogen stream; and

Passing the treated hydrogen stream to mix with the crude oil upstream of the hydroprocessing reactor.

12. the method of any one of the preceding claims, further comprising passing pyrolysis oil produced in the separator to the gasifier, wherein the gasifier converts at least a portion of the pyrolysis oil to hydrogen gas.

13. The method of any of the preceding claims, further comprising preheating the crude oil to a temperature of at least 300 ℃ prior to entering the hydroprocessing reactor.

14. The process of any preceding claim, wherein the higher boiling fraction comprises vacuum resid.

15. The method of any one of the preceding claims, wherein the gasifier produces hydrogen, carbon monoxide, a heated stream, or a combination thereof.

Technical Field

Embodiments of the present disclosure relate to systems and methods for producing olefinic and aromatic petrochemicals from crude oil, and in particular to systems and methods for producing olefinic and aromatic petrochemicals from crude oil using a hydroprocessing reactor.

Background

Olefins (e.g., ethylene, propylene, butylene, butadiene) and BTX (benzene, toluene and xylene) are basic and essential intermediates in the petrochemical industry. It is produced mainly by thermal cracking (or steam pyrolysis) of petroleum gases and distillates such as naphtha, kerosene or even gaseous oils. To obtain high yields of olefins and BTX, the preferred feed to the steam cracker should be a highly paraffinic and low aromatic content feed, as these feed characteristics help to reduce undesirable products and coke formation.

By upgrading the crude oil in a hydrotreating reactor, the linear paraffin properties are improved and can be fed directly to a steam cracker, enabling the production of greater amounts of olefins and aromatics directly from the crude oil.

Disclosure of Invention

To ensure that the crude oil is converted to a feed having the desired amount of paraffins and a minimal amount of aromatics, there is a significant hydrogen requirement for the hydroprocessing reactor or the crude conditioning unit. Although the steam cracker unit produces hydrogen that can be recycled to the hydroprocessing reactor, the amount of recycled hydrogen from the steam cracker does not make the system self-sufficient in terms of its hydrogen requirements. Thus, there is a continuing need for a self-sufficient system for generating sufficient hydrogen for a hydroprocessing reactor.

Embodiments of the present disclosure increase hydrogen production for a hydroprocessing reactor by gasifying undesirable crude oil fractions to produce hydrogen. In crude oil conversion processes, about 10 to 15 weight percent (wt%) of the low value, high boiling (e.g., 540 ℃ and higher) fraction (hereinafter "higher boiling fraction") must be discharged to reduce coke formation in the steam cracker. Embodiments of the present disclosure use this higher boiling fraction as a feed to a gasification unit to produce more hydrogen and generate power. In addition to the pyrolysis hydrogen, the hydrogen produced from the gasification unit enables the crude oil conversion process of the present invention to be self-sufficient in terms of hydrogen demand.

According to one embodiment, petrochemicals may be produced from crude oil by a process that may include passing crude oil and hydrogen into a hydroprocessing reactor, separating the hydroprocessed oil into a lower boiling fraction and a higher boiling fraction, passing the lower boiling fraction to a pyrolysis section of a steam cracker to produce a pyrolysis effluent comprising olefins, aromatic hydrocarbons, or both, and passing the higher boiling fraction to a gasifier. The gasifier may produce hydrogen, and at least a portion of the hydrogen produced by the gasifier may be passed to the hydrotreating reactor. The hydroprocessing reactor contains one or more hydroprocessing catalysts that produce hydroprocessed oil.

According to another embodiment, a method for producing olefinic and aromatic petrochemicals is provided. The method includes mixing hydrogen with crude oil to produce a feed stream comprising hydrogen and crude oil, and passing the crude oil and hydrogen mixture to a hydroprocessing reactor operating at a temperature of 300 ℃ to 450 ℃ and a hydrogen partial pressure of 30 to 200 bar, the hydroprocessing reactor comprising a hydroprocessing catalyst that produces a hydroprocessed mixture from the crude oil and hydrogen mixture. Passing the hydrotreated mixture to at least one steam cracker comprising a convection section operated at a temperature of 700 ℃ to 900 ℃ to produce a heated hydrotreated mixture, separating the mixture into a lower boiling fraction and a higher boiling fraction. Passing the lower boiling fraction to a pyrolysis section of a steam cracker downstream of the convection section to produce a pyrolysis effluent comprising olefins and aromatic hydrocarbons, and passing the pyrolysis effluent to at least one separator, wherein the separator converts the pyrolysis effluent into one or more product streams comprising olefins, aromatic hydrocarbons, or a combination thereof. Passing the higher boiling fraction to a gasifier operating at a temperature of at least 900 ℃, wherein the gasifier produces hydrogen and the hydrogen produced in the gasifier is recycled for mixing with the crude oil upstream of the hydroprocessing reactor.

Drawings

Fig. 1 is a schematic depiction of a crude oil conversion system according to one or more embodiments of the present disclosure.

Fig. 2 is another schematic depiction of a crude conversion system according to one or more embodiments of the present disclosure.

Fig. 3 is yet another schematic depiction of a crude conversion system in accordance with one or more embodiments of the present disclosure.

Fig. 4 is another schematic depiction of a crude conversion system according to one or more embodiments of the present disclosure.

For purposes of describing the simplified schematic illustration and description of fig. 1-4, a wide variety of valves, temperature sensors, electronic controllers, etc. that may be employed and are well known to those of ordinary skill in the art of certain chemical processing operations are not included. In addition, accompanying components such as air supplies, catalyst hoppers, and flue gas handling devices, as often included in typical chemical treatment operations of a refinery, are not depicted. It should be understood that these components are within the spirit and scope of the disclosed embodiments of the invention. However, operational components, such as those described in this disclosure, may be added to the embodiments described in this disclosure.

Reference will now be made in detail to various embodiments, some of which are illustrated in the accompanying drawings. Wherever possible, the same reference numbers will be used throughout the drawings to refer to the same or like parts.

The embodiments set forth in the drawings are illustrative in nature and not intended to limit the claims. Furthermore, individual features of the drawings will become more apparent and appreciated by the detailed description.

Additional features and advantages of the embodiments will be set forth in the detailed description which follows, and in part will be readily apparent to those skilled in the art from that description or recognized by practicing the embodiments described herein, including the detailed description which follows, the claims, as well as the appended drawings.