Method and system for processing hydrocarbon-containing mixtures

Abstract

A method and system for treating a hydrocarbon-containing mixture is disclosed, which comprises the following steps: I) separating the hydrocarbon-containing mixture into light and heavy components; II) reacting the light fraction obtained in step I) in an aromatization unit to produce a reaction product of C5 - Ingredients and C6 + III) in an aromatics conversion unit, separating the heavy components obtained in step I) and, optionally, the C6 + The components are reacted to form the reaction product, - component, C6-C7 component, C8 component, and C9 + and IV) optionally separating the C5 - Components and C5 obtained in step III - The process includes steam cracking or catalytic cracking of one or both of the components. The process and system can convert low-value hydrocarbon mixtures into C aromatic hydrocarbons and cracked feedstocks, thereby increasing the value of the products.

Description

Detailed Description of the Invention

[0001] CROSS-REFERENCE TO RELATED APPLICATIONS This application claims priority to Chinese Patent Application No. 202011104622.0, filed on October 15, 2020, entitled "System and Method for Utilizing Hydrocarbon-Containing Mixtures," the contents of which are incorporated herein by reference in their entirety.

[0002] [Technical Field] FIELD OF THE INVENTION This application relates to hydrocarbon processing, and in particular to methods and systems for processing hydrocarbon-containing mixtures.

[0003] [Background technology] Aromatics and olefins are the basic raw materials for the petrochemical industry. Paraxylene is the main aromatic hydrocarbon product, with a domestic supply gap of more than 1 billion tons per year. Ethylene and propylene have large supply-demand gaps. Accelerating the development of the aromatics and olefins industry is essential for the development of China's basic chemical industry. Industrial plants mainly use naphtha as raw material and produce aromatic hydrocarbons through catalytic reforming, which are then converted into toluene / benzene and C9 + A is converted to xylenes through isomerization and transalkylation units. Furthermore, China's steam cracking plants for producing light olefins also mainly use naphtha as a raw material, so the raw materials for aromatics and olefins compete with each other, and the raw materials costs for aromatics and olefins are high. Therefore, the search for lower-cost and more diverse raw materials for aromatics and olefins is an important factor in resolving the bottleneck in aromatics and olefins production in the future.

[0004] With the use and popularization of new energy technologies and the upgrading of gasoline in China, the demand for automobile gasoline will tend to decrease in the future, and the requirements for the aromatics and olefins content in gasoline will further decrease. Therefore, converting part of low-grade gasoline into high-value C8 aromatics and co-producing olefins is an effective way to expand the use of gasoline and alleviate the shortage of raw materials for producing p-xylene.

[0005] Chinese Patent Publication CN101767035B discloses a catalyst for producing BTX aromatic hydrocarbons by catalytic cracking of gasoline and its preparation, the catalyst comprising 0.05-2.0 wt% of a Group VIII noble metal, 0.2-5.0 wt% of Zn, 0.2-5.0 wt% of Sn, and 5.0-80 wt% of a ZSM-5 / ZSM-11 co-crystallized molecular sieve, has good aromatization activity, BTX selectivity, sulfur tolerance, and olefin tolerance, and can be used to produce aromatic hydrocarbons from catalytically cracked gasoline and / or straight-run gasoline, or can be blended with gasoline fractions such as coking gasoline and cracked gasoline.

[0006] Chinese Patent Application Publication CN1923965A discloses a method for producing ethylene, propylene, and aromatic hydrocarbons from catalytic cracking gasoline, in which the feedstock is contacted with a catalyst once to convert it into a mixture of ethylene, propylene, and aromatic hydrocarbons.

[0007] However, the existing methods still have the problem of low comprehensive utilization of hydrocarbon mixtures and low value of the products.

[0008] Summary of the Invention The object of the present application is to provide a novel method and system for processing hydrocarbon mixtures that can achieve efficient and comprehensive utilization of the hydrocarbon mixture and improve the value of the products.

[0009] To achieve the above object, in one aspect, the present application provides a method for treating a hydrocarbon-containing mixture, comprising the steps of: I) separating the hydrocarbon-containing mixture into a light fraction and a heavy fraction, wherein the light fraction is C7 - The heavy fraction is C8 + or the light fraction is a C5 - The heavy fraction is a C6 + is an ingredient; II) in an aromatization unit, the light fraction from step I) is reacted to form the resulting reaction product into C5 - Ingredients and C6 + and separating the components, wherein the reaction occurring in the aromatization unit comprises an aromatization reaction; III) in an aromatics conversion unit, the heavy fraction from step I) and, optionally, the C6 + The components are reacted, and the resulting reaction product is - The fraction, C6-C7 components, C8 components, and C9 + wherein the reaction occurring in the aromatic conversion unit comprises a transalkylation reaction; and IV) optionally, the C5 from step II) - Component and said C5 from step III) - Catalytically cracking at least a portion of one or both of the components or subjecting it to steam cracking, optionally after hydrosaturation.

[0010] Preferably, the method further comprises one or both of the following steps: V) purifying the C8 components from step III) to obtain C8 aromatic hydrocarbons and non-aromatic components, and optionally purifying at least a portion of the obtained non-aromatic components to the C5 - dissolving together with the ingredients; and VI) The C6 to C7 components and the C9 +recycling at least a portion of one or more of the components to said aromatic conversion unit of step III) for further reaction.

[0011] In another aspect, the present application provides a method for treating a hydrocarbon-containing mixture, comprising the steps of: 1) separating the hydrocarbon-containing mixture into a light fraction and a heavy fraction, wherein the light fraction is C7 - The heavy fraction is C8 + or the light fraction is a C5 - The heavy fraction is a C6 + is an ingredient; 2) reacting the light fraction from step 1) in the presence of an aromatization catalyst to form the resulting reaction product into a C5 - Ingredients and C6 + Separating the components; 3) in the presence of an aromatics conversion catalyst, the heavy fraction from step 1) and, optionally, the C6 + The components are reacted, and the resulting reaction product is - component, C6-C7 component, C8 component, and C9 + separating the components; and 4) optionally, the C5 from step 2) - Ingredients and the C5 from step 3) - Catalytically cracking at least a portion of one or both of the components or subjecting it to steam cracking, optionally after hydrosaturation.

[0012] Preferably, the method further comprises one or both of the following steps: 5) purifying the C8 components from step 3) to obtain C8 aromatic hydrocarbons and non-aromatic components, and optionally purifying at least a portion of the non-aromatic components from step 4) to obtain C5 aromatic hydrocarbons and non-aromatic components. - dissolving together with the ingredients; and 6) The C6 to C7 components and the C9 components from step 3) +Recycle at least a portion of one or more of the components for further reaction in the presence of said aromatics conversion catalyst in step 3).

[0013] In yet another aspect, the present application provides a system for carrying out the method for treating a hydrocarbon-containing mixture according to the present application, comprising: a separation unit for separating the hydrocarbon-containing mixture into the light fraction and the heavy fraction; The light fraction from the separation unit is reacted and the resulting reaction product is separated to obtain C5 - Components, and C6 + aromatization unit to obtain ingredients; the heavy fraction from the separation unit, and optionally the C6 + The components are reacted and the resulting reaction products are separated to form C5 - components, C6-C7 components, C8 components, and C9 + aromatic conversion unit to obtain components; Optionally, the C5 - component and the C5 - a cracking unit for catalytically cracking at least a portion of one or both of the components or subjecting it to steam cracking, optionally after hydrosaturation; and Optionally, the C5 - component and the C5 - A hydrogenation saturation unit for hydrogenating at least a portion of one or both of the components to saturation.

[0014] Preferably, the system further comprises an aromatics purification unit for purifying the C8 components from the aromatics conversion unit to obtain C8 aromatic hydrocarbons and non-aromatic components.

[0015] In the method and system according to the present application, after the separation of the hydrocarbon-containing mixture, the light fraction rich in alkanes and olefins is subjected to aromatization reaction to convert non-aromatic components into aromatic hydrocarbon products, while the resulting by-product light hydrocarbons can be used as a high-quality feedstock for the production of light olefins; the heavy fraction rich in aromatic hydrocarbons is subjected to reactions such as hydrocracking, transalkylation, etc. to convert benzene, toluene, and heavy aromatics into C aromatic hydrocarbons, while the resulting by-product light hydrocarbons can be used as a high-quality feedstock for the production of light olefins; and finally, the C aromatic hydrocarbons can be purified in an aromatics purification unit. Through the above process, the low-value hydrocarbon mixture can be converted into C aromatic hydrocarbons and cracked feedstock, thereby improving the value of the product.

[0016] By using the method according to the present invention, the content of aromatics in the reaction product of the aromatization unit is increased by 15% or more, preferably 20% or more, compared with the feedstock; the content of C8 aromatics in the reaction product of the aromatic conversion unit is increased by at least 20%, preferably at least 30%, compared with the feedstock; the purity of the C8 aromatic hydrocarbon product of the aromatic purification unit can approach 99% or more; and the obtained C5 - The light hydrocarbon components can be used directly as cracking feedstock or can be used as steam cracking feedstock after hydrosaturation.

[0017] Other features and advantages of the present application are explained in detail in the detailed description herein below.

[0018] BRIEF DESCRIPTION OF THE DRAWINGS The drawings that form part of this specification are provided to aid in the understanding of the application and should not be considered limiting. The application can be read with reference to the drawings in combination with the following detailed description. In the drawings: FIG. 1 is a schematic flow diagram of a preferred embodiment of the method according to the present application; FIG. 2 is a schematic flow diagram of another preferred embodiment of the method according to the present application; FIG. 3 is a schematic flow diagram of another preferred embodiment of the method according to the present application; Figure 4 shows the NH3-TPD pattern of the catalyst obtained in Preparation Example 1 of the present application; FIG. 5 shows a TEM image of the catalyst obtained in Preparation Example 1 of the present application.

[0019] Detailed Description of the Invention The present application will be described in more detail below with reference to the drawings and specific embodiments thereof. It should be noted that the specific embodiments of the present application are provided for illustrative purposes only and are not intended to be limiting in any way.

[0020] Any specific numerical value, including the endpoints of a numerical range, described in the context of this application should not be limited to that exact value, but should also be interpreted as encompassing all values ​​close to that exact value, for example, all values ​​within ±5% of that exact value. Furthermore, with respect to any numerical range described herein, any combination between the endpoints of the range, between each endpoint and any particular value within the range, or between any two particular values ​​within the range, can be made to provide one or more new numerical ranges, which new numerical ranges should also be considered to be specifically described in this application.

[0021] Unless otherwise specified, terms used herein have the same meaning as commonly understood by one of ordinary skill in the art; where a term is defined herein and that definition differs from the common understanding in the art, the definition provided herein shall prevail.

[0022] In the context of this application, C5 - The component refers to hydrocarbon components with a boiling point lower than that of benzene; C6 + The component refers to hydrocarbon components with boiling points not lower than benzene; C7 - The component refers to hydrocarbon components with a boiling point lower than that of toluene, and is C8 +The component refers to a hydrocarbon component with a boiling point higher than toluene.

[0023] In the context of this application, C6-C7 components refer to hydrocarbon components having a boiling point between the boiling point of benzene and the boiling point of xylene; whereas, C8 components refer to hydrocarbon components having a boiling point near (e.g., ±10°C) the boiling point of xylene; and C9 + The component refers to a hydrocarbon component having a boiling point higher than that of xylene.

[0024] In the context of this application, high purity C8 aromatic hydrocarbons refer to C8 aromatic hydrocarbons that meet the purity requirements for adsorptive or crystallization separation of para-xylene, which requirements are typically greater than 99%.

[0025] In this application, the medium to strong acid content of the catalyst is calculated according to the peak area within the temperature range of 200-400°C in its NH3-TPD pattern; the ratio of the medium to strong acid content to the total acid content refers to the ratio of the peak area within the temperature range of 200-400°C to the total peak area within the temperature range of 100-600°C in the NH3-TPD pattern.

[0026] In the context of this application, unless otherwise indicated, all pressures refer to gauge pressures.

[0027] In the context of this application, in addition to the explicitly stated subject matter, any subject matter or unmentioned subject matter shall be considered to be the same as that known in the art without any modifications.In addition, any of the embodiments described herein can be freely combined with one or more embodiments described herein, and the technical solutions or ideas thus obtained shall be considered as part of the original disclosure or original description of this application, and shall not be considered as new matters not disclosed or anticipated herein, unless it is obvious to those skilled in the art that such combination is obviously unreasonable.

[0028] All patent and non-patent literature cited herein, including but not limited to textbooks and journal articles, is hereby incorporated by reference in its entirety.

[0029] As noted above, in a first aspect, the present invention provides a method for treating a hydrocarbon-containing mixture, the method comprising the steps of: I) separating the hydrocarbon-containing mixture into a light fraction and a heavy fraction, wherein the light fraction is C7 - The heavy fraction is C8 + or the light fraction is a C5 - The heavy fraction is a C6 + is an ingredient; II) in an aromatization unit, the light fraction from step I) is reacted to form the resulting reaction product into C5 - Ingredients and C6 + and separating the components, wherein the reaction occurring in the aromatization unit comprises an aromatization reaction; III) in an aromatics conversion unit, the heavy fraction from step I) and, optionally, the C6 + The components are reacted, and the resulting reaction product is - Fraction, C6-C7 components, C8 components, and C9 + wherein the reaction occurring in the aromatic conversion unit comprises a transalkylation reaction; and IV) optionally, the C5 from step II) - Component and said C5 from step III) - Catalytically cracking at least a portion of one or both of the components or subjecting it to steam cracking, optionally after hydrosaturation.

[0030] In a preferred embodiment, the method further comprises one or both of the following steps: V) purifying the C8 components from step III) to obtain C8 aromatic hydrocarbons and non-aromatic components, and optionally purifying at least a portion of the obtained non-aromatic components to the C5 -dissolving together with the ingredients; and VI) The C6 to C7 components and the C9 + recycling at least a portion of one or more of the components to said aromatic conversion unit of step III) for further reaction.

[0031] In a second aspect, the present application provides a method for treating a hydrocarbon-containing mixture, comprising the steps of: 1) separating the hydrocarbon-containing mixture into a light fraction and a heavy fraction, wherein the light fraction is C7 - The heavy fraction is C8 + or the light fraction is a C5 - The heavy fraction is a C6 + is an ingredient; 2) reacting the light fraction from step 1) in the presence of an aromatization catalyst to form the resulting reaction product into a C5 - Ingredients and C6 + Separating the components; 3) in the presence of an aromatics conversion catalyst, the heavy fraction from step 1) and, optionally, the C6 + The components are reacted, and the resulting reaction product is - component, C6-C7 component, C8 component, and C9 + separating the components; and 4) optionally, the C5 from step 2) - Ingredients and the C5 from step 3) - Catalytically cracking at least a portion of one or both of the components or subjecting it to steam cracking, optionally after hydrosaturation.

[0032] In a preferred embodiment, the method further comprises one or both of the following steps: 5) purifying the C8 components from step 3) to obtain C8 aromatic hydrocarbons and non-aromatic components, and optionally purifying at least a portion of the non-aromatic components from step 4) to obtain C5 aromatic hydrocarbons and non-aromatic components. - dissolving together with the ingredients; and 6) The C6 to C7 components and the C9 components from step 3) + Recycle at least a portion of one or more of the components for further reaction in the presence of said aromatics conversion catalyst in step 3).

[0033] According to the present application, the separation in steps I) / 1), II) / 2), and III) / 3) is carried out by separating the mixture into components having different boiling points or boiling ranges according to their boiling points by distillation, rectification, or fractionation. For example, in step I) / 1), the hydrocarbon-containing mixture is separated into C7 - Ingredients and C8 + or by separation in a distillation column, C5 - Ingredients and C6 + The specific separation conditions used in step II) / step 2) and step III) / step 3) can be easily determined by one skilled in the art taking into account the target components to be separated, and a detailed description thereof will be omitted herein for the sake of brevity.

[0034] The hydrocarbon-containing mixture suitable for use herein may be a variety of hydrocarbon mixtures containing C3 to C12 hydrocarbons, but one or more of the C3 to C12 hydrocarbons may be absent, as long as the separation of the mixture into light and heavy fractions in step I) or step 1) is not affected. In a preferred embodiment, the hydrocarbon-containing mixture has a distillation range of 40 to 300°C, more preferably 50 to 250°C. In a more preferred embodiment, the hydrocarbon-containing mixture is selected from the group consisting of catalytically cracked gasoline, hydrocracked gasoline, ethylene-cracked gasoline, straight-run naphtha, catalytic reformate, LPG, any mixture thereof, or other fractions with a similar composition, such as catalytic diesel or their hydrocracking products.

[0035] In a preferred embodiment, the hydrocarbon-containing mixture has one or more of the following properties: sulfur content of 0.5-4 ppm by weight; Nitrogen content of 0-2 ppm by weight; Aromatic content of 15-45 wt%; an olefin content of 20 to 45 wt.%; and Alkane content is 20-40% by weight.

[0036] The hydrocarbon-containing mixture according to the preferred embodiment described above can be more efficiently utilized by treating it with the method according to the present application.

[0037] According to the present invention, after separation of the hydrocarbon-containing mixture, the light fraction rich in alkanes and olefins is subjected to aromatization reaction to convert non-aromatic components into aromatic hydrocarbon products, while the resulting by-product light hydrocarbons can be used as a high-quality feedstock for the production of light olefins; the heavy fraction rich in aromatic hydrocarbons is subjected to reactions such as hydrocracking and transalkylation to convert benzene, toluene, and heavy aromatics into C aromatic hydrocarbons, while the resulting by-product light hydrocarbons can be used as a high-quality feedstock for the production of light olefins. The C aromatic hydrocarbons can be purified, for example, in an aromatics purification unit, to obtain high-purity C aromatic hydrocarbons. Through the above process, the low-value hydrocarbon mixture can be converted into C aromatic hydrocarbons and cracking feedstock for the production of light olefins in the method according to the present invention, thereby improving the value of the product.

[0038] In a preferred embodiment, the aromatic content of the reaction product of step II) and step 2) is increased by 15% or more compared to the feedstock, and more preferably, the aromatic content of the reaction product is increased by 20% or more compared to the feedstock.

[0039] In a preferred embodiment, the content of C8 aromatics in the reaction product of step III) and step 3) is increased by at least 20% compared to the feedstock; more preferably, the content of C8 aromatics in the reaction product is increased by at least 30% compared to the feedstock.

[0040] In a preferred embodiment, the C8 aromatic product obtained in step V) and step 5) has a purity of more than 99% by weight.

[0041] In the present application, the aromatization catalyst used in the aromatization unit of step II) and the aromatization catalyst used in step 2) may be conventional, and may contain, for example, 50 to 90 wt % of a molecular sieve, which may be selected from the group consisting of aluminosilicates, aluminogallosilicates, aluminosilicophosphates, aluminoferrosilicates, and combinations thereof, having a pore structure of 10 or 12 rings, and 0.5 to 10 wt % of a modifying metal, which may be selected from the group consisting of Group IB metals, Group IIB metals, Group VIB metals, Group VIIB metals, Group VIII metals, and combinations thereof.

[0042] In a preferred embodiment, the reaction conditions in step II) and step 2) are a reaction temperature of 400 to 600°C, a reaction pressure of 0.2 to 3 MPa, and a reaction time of 0.5 to 5 hours. -1 Including the feed space velocity.

[0043] In the present application, the aromatic conversion catalyst used in the aromatic conversion unit of step III) and the aromatic conversion catalyst used in step 3) can be a conventional aromatic conversion catalyst, for example: The composition may comprise 50 to 90 wt. % of a molecular sieve, which may be selected from the group consisting of aluminosilicates having a 10- or 12-membered ring pore structure, such as ZSM-5 molecular sieve, ZSM-12 molecular sieve, MCM-22 molecular sieve, MOR molecular sieve, and β molecular sieve, and 0.05 to 10 wt. % of a modifying metal, which may be selected from the group consisting of Group VB metals, Group VIB metals, Group IIB metals, Group VIII metals, or metal oxides thereof, preferably Pt, Mo, and Re.

[0044] In a preferred embodiment, the aromatic conversion catalyst comprises a molecular sieve component, an active metal component, and an oxide additive, wherein the active metal component is fixed on the molecular sieve component and may be in the form of a metal element and / or a metal oxide, the active metal in the active metal component is selected from the group consisting of Group VB metals, Group VIB metals, and Group VIIB metals, the molecular sieve component is at least one selected from the group consisting of MCM-22 molecular sieve, MOR molecular sieve, and ZSM-12 molecular sieve, and the catalyst has a medium-strong acid content of 0.05 to 2.0 mmol / g catalyst, and the ratio of the medium-strong acid content to the total acid content is 60 to 99%.

[0045] In a preferred embodiment, the catalyst has a medium-strong acid content of 0.1 to 1 mmol / g, and the ratio of the medium-strong acid content to the total acid content is 68 to 92%.

[0046] In the present invention, due to the hydrogen transfer effect of the metal surface and the synergistic effect between the metal surface and the acid sites of the molecular sieve, the metal component fixed on the surface of the molecular sieve can preferentially cover or weaken part of the strong acid center, thereby exerting a synergistic effect with the neighboring acid sites of the molecular sieve, thereby promoting the transalkylation reaction and the isomerization reaction and reducing the deep hydrocracking side reaction.

[0047] In a preferred embodiment, the active metal component is immobilized on the molecular sieve component by physical mixing and chemical bonding.

[0048] In a preferred embodiment, the molecular sieve component is present in an amount of 50 to 90 wt %, preferably 60 to 80 wt %, the oxide additive is present in an amount of 5 to 40 wt %, preferably 20 to 40 wt %, and the active metal component, calculated as elemental metal, is present in an amount of 0.01 to 10 wt %, preferably 0.1 to 8 wt %, based on 100% total weight of the catalyst.

[0049] According to the present application, any active metal that satisfies the requirements described herein can be used. For example, the active metal is selected from the group consisting of Group VB metals, Group VIB metals, and Group VIIB metals, and is preferably one or more of Mo, W, and Re; more preferably at least two of Mo, Re, and W, where the mixed weight ratio calculated as metal elements is 0.1 to 10:1; or a combination of Mo, Re, and W, where the weight ratio of Mo to Re to W is 1:0.1-0.4:0.1-0.6.

[0050] According to the present application, the oxide additives can be selected within a wide range, and all conventional oxide additives can be used in the present application, preferably one or more selected from the group consisting of alumina, silica, magnesia, titania, zirconia, and kaolin.

[0051] According to the present application, the aromatic conversion catalyst preferably further comprises a phosphorus-containing component, more preferably the phosphorus-containing component is fixed on the molecular sieve component by physical mixing and / or chemical bonding, and the phosphorus content calculated as P2O5 is preferably 0.1-5 wt%.

[0052] Any aromatic conversion catalyst that meets the above-mentioned requirements of the present application can be used, and its preparation method is not particularly limited. In a preferred embodiment, the aromatic conversion catalyst can be prepared by the following steps: a) fixing an active metal and / or an active metal oxide on a molecular sieve; and b) kneading the product from step a) with an oxide additive to form a catalyst. In the present application, the active metal and / or an active metal oxide is fixed on a molecular sieve and then kneaded with an oxide additive to form a catalyst. The synergistic effect of the metal with the acid center of the molecular sieve and the adjusting effect of the metal on the acidity provide a specific distribution of the active metal on the catalyst, which can effectively reduce the strong acid center of the molecular sieve and effectively increase the medium-to-strong acid center of the molecular sieve, thereby promoting the addition efficiency of aromatic hydrocarbons, improving xylene selectivity, and inhibiting deep hydrocracking side reactions.

[0053] In a more preferred embodiment, the aromatic conversion catalyst can be prepared by a method including: (a) impregnating a molecular sieve component source with an active metal source solution and heat-treating the resultant to obtain a modified molecular sieve; and (b) kneading the modified molecular sieve with an oxide additive source to form the modified molecular sieve. In the present application, the impregnation may be isochoric impregnation or supersaturated impregnation, and preferably supersaturated impregnation.

[0054] In a further preferred embodiment, in step a), the heat treatment comprises a roasting step or a combination of a drying step and a roasting step, preferably a combination of a drying step and a roasting step.

[0055] In the present application, the drying conditions can be selected within a wide range, and all conventional drying conditions can be used in the present application. Preferred drying conditions include a temperature of 50 to 200°C and a drying time (preferably 1 to 30 hours) that can be adjusted depending on the temperature.

[0056] In the present application, the roasting conditions can be selected within a wide range, and all conventional roasting conditions can be used in the present application. Preferred roasting conditions include a temperature of 300 to 700°C and a drying time (preferably 1 to 30 hours) that can be adjusted depending on the temperature. More preferably, the roasting step is carried out in an oxygen-containing atmosphere such as air, and particularly preferably, the oxygen-containing atmosphere is a mixed gas of air and steam in a volume ratio of 5 to 100:1.

[0057] According to the present application, the active metal source can be selected within a wide range and can be, for example, a soluble compound of the active metal, preferably a soluble compound containing a metal selected from Group VB metals, Group VIB metals, and Group VIIB metals, such as nitrates, chlorides, sulfates, and ammonium salts, the detailed description of which is omitted here for the sake of brevity. In the present application, the source of oxide additives may be, for example, one or more selected from the group consisting of alumina, silica, magnesia, titania, and kaolin, or precursors thereof.

[0058] According to the present application, step a) is preferably carried out in the presence of a phosphorus source, and more preferably, the phosphorus source is a soluble compound, the type of which is not particularly limited, for example, phosphoric acid, ammonium hydrogen phosphate, and ammonium dihydrogen phosphate, the detailed description of which is omitted herein for the sake of brevity.

[0059] The aromatic conversion catalyst of the present invention has advantages such as high reaction activity and low loss rate of aromatic hydrocarbons when used in aromatic conversion.

[0060] The aromatic conversion catalyst of the present application can be reduced before use as needed. The reduction step has no specific requirements and can be carried out, for example, by introducing hydrogen for reduction or by using other reducing agents, and detailed descriptions thereof are omitted herein for the sake of brevity.

[0061] In a preferred embodiment, the reaction conditions in step III) and step 3) are a reaction temperature of 250 to 500°C, a reaction pressure of 1.5 to 6.5 MPa, a molar ratio of hydrogen to hydrocarbon of 1 to 10, and a reaction time of 0.5 to 5 hours. -1 The feed weight hourly space velocity (WHSV) is calculated based on the weight of the feed gas per unit of time.

[0062] According to the present application, the steam cracking and catalytic cracking in steps IV) and 4) can be carried out by conventional methods, and there are no specific requirements in the present application. In a specific preferred embodiment, the operating conditions for the steam cracking in steps IV) and 4) include a cracking temperature of 600 to 1000°C, a residence time of 0.01 to 0.8 seconds, and a reaction pressure of 0.1 to 0.3 MPa (G). In another preferred embodiment, the catalytic cracking in steps IV) and 4) is carried out in the presence of a catalyst comprising a USY molecular sieve, a ZSM-5 molecular sieve, or a β molecular sieve; more preferably, the operating conditions for the catalytic cracking are a reaction temperature of 450 to 650°C, a residence time of 0.5 to 20 hours, and a pressure of 0.1 to 0.3 MPa (G). -1 a weight hourly space velocity of 0.05 to 0.5 MPa, a reaction pressure of 0.05 to 0.5 MPa, a mass ratio of catalyst to oil of 0.1 to 10, and preferably a reaction temperature of 500 to 600°C, a reaction time of 1 to 10 hours-1 weight hourly space velocity of 0.1-0.3 MPa, reaction pressure of 0.1-0.3 MPa, and catalyst to oil ratio of 0.3-6.

[0063] In a preferred embodiment, the cracked feedstock is subjected to hydrosaturation in steps IV) and 4) before steam cracking. The operating conditions for hydrosaturation can be selected within a wide range. The main purpose of hydrosaturation is to saturate the olefin components in the feedstock to increase the alkane components of the product, thereby promoting an improvement in the yield of olefin products in the subsequent steam cracking.

[0064] In a preferred embodiment, the operating conditions for the hydrogenation saturation are a reaction temperature of 150 to 600°C, a reaction pressure of 0.5 to 6 MPa, and a reaction time of 0.5 to 10 hours. -1 and a volumetric ratio of hydrogen to hydrocarbon of 200 to 2000.

[0065] According to the present application, the catalyst used for the hydrosaturation may be a conventional one. For example, the catalyst may contain 0.1 to 20 wt % of a metal component which is one or more selected from the group consisting of Ni, Mo, Co, Pt, and Pd, and 80 to 99.9 wt % of a support component which is one or more selected from the group consisting of alumina, kaolin, magnesia, silica, titania, calcium oxide, and amorphous silica-alumina.

[0066] In a preferred embodiment, the purification in step V) and step 5) is aromatic extractive separation, non-aromatics selective cracking, or a combination thereof.

[0067] According to the present application, aromatic extractive separation can be carried out by conventional methods, and there are no specific requirements in the present application. In a preferred embodiment, aromatic extractive separation is carried out by extractive distillation using sulfolane solvent.

[0068] According to the present application, the non-aromatic selective cracking can be carried out by a conventional method, and there are no specific requirements in the present application. In a preferred embodiment, the non-aromatic selective cracking is carried out in the presence of a catalyst containing 50 to 80 wt. % of a molecular sieve, which is at least one of ZSM-5 molecular sieve, MCM-22 molecular sieve, MOR molecular sieve, and β molecular sieve, and optionally 0.1 to 10 wt. % of a metal component containing a metal selected from Group VIB metals, Group VIIB metals, and Group VIII metals. More preferably, the operating conditions for the non-aromatic selective cracking are a reaction temperature of 300 to 600°C, a reaction pressure of 0.5 to 3.0 MPa, a molar ratio of hydrogen to hydrocarbon of 1 to 10, and a reaction time of 1 to 15 hours. -1 The feed weight hourly space velocity (WHSV) is calculated based on the weight of the feed gas per unit of time.

[0069] In a second aspect, the present application provides a system for carrying out the method for treating a hydrocarbon-containing mixture according to the present application, comprising: a separation unit for separating the hydrocarbon-containing mixture into the light fraction and the heavy fraction; The light fraction from the separation unit is reacted and the resulting reaction product is separated to obtain C5 - Components and C6 + aromatization unit to obtain ingredients; the heavy fraction from the separation unit, and optionally the C6 + The components are reacted and the resulting reaction products are separated to form C5 - components, C6-C7 components, C8 components, and C9 + aromatic conversion unit to obtain components; Optionally, the C5 - component and the C5 - a cracking unit for catalytically cracking at least a portion of one or both of the components or subjecting it to steam cracking, optionally after hydrosaturation; and Optionally, the C5 - component and the C5 -A hydrogenation saturation unit for hydrogenating at least a portion of one or both of the components to saturation.

[0070] In some embodiments, the separation unit comprises a hydrocarbon-containing mixture inlet, a light ends outlet, and a heavy ends outlet; and the aromatization unit comprises an inlet, a C5 - Component outlet, and C6 + and a component outlet; the aromatic conversion unit includes an inlet, a C5 - Component outlet, C6-C7 component outlet, C8 component outlet, and C9 + the cracking unit has an inlet and a cracked product outlet; the light end outlet of the separation unit is in communication with the inlet of the aromatization unit, the heavy end outlet of the separation unit is in communication with the inlet of the aromatics conversion unit, and the C5 - The component outlet and the C5 - One or both of the component outlets are in communication with the inlet of the cracking unit, optionally through the hydrosaturation unit.

[0071] In a preferred embodiment, the system further comprises an aromatics purification unit for purifying the C8 components from the aromatics conversion unit to obtain C8 aromatic hydrocarbons and non-aromatic components; Preferably, the aromatics purification unit comprises an inlet, a C8 aromatic hydrocarbon outlet, and a non-aromatic component outlet, the C8 component outlet of the aromatics conversion unit being in communication with the inlet of the aromatics purification unit, and the non-aromatic component outlet of the aromatics purification unit being in communication with the inlet of the cracking unit, optionally through the hydrosaturation unit.

[0072] In a preferred embodiment, the cracking unit may be a steam cracking unit, a catalytic cracking unit, or a combination thereof.

[0073] In a preferred embodiment, the aromatic purification unit can be an aromatic extraction separation unit, a non-aromatic selective cracking unit, or a combination thereof.

[0074] According to the present application, the separation unit may be in the form of a distillation, rectification or fractionation column commonly used in the art, such as a vacuum rectification column, an atmospheric rectification column or a pressure rectification column.

[0075] According to the present application, the aromatization unit may be in the form of an aromatization reactor commonly used in the art, such as a fixed bed reactor or a moving bed reactor.

[0076] According to the present application, the aromatic conversion unit may be in the form of a fixed bed reactor, such as an axial fixed bed reactor, commonly used in the art.

[0077] According to the present application, the steam cracking unit may be in the form of a millisecond furnace or a conventional cracking furnace commonly used in the art, such as an ultra-short residence time cracking furnace, a short residence time cracking furnace, etc.

[0078] According to the present application, the catalytic cracking unit may be in the form of a catalytic cracking reactor commonly used in the art, such as a fixed bed reactor, a fluidized bed reactor, or a riser reactor.

[0079] According to the present application, said hydrogenation saturation unit may be in the form of a fixed bed reactor commonly used in the art, such as an axial fixed bed reactor.

[0080] According to the present application, the aromatic extraction separation unit can be in the form of a liquid-liquid extractor, extractive distillation column, etc. commonly used in the art, such as an extractive distillation column using sulfolane solvent.

[0081] According to the present application, the non-aromatic selective cracking unit may be in the form of a fixed bed reactor commonly used in the art, such as an axial fixed bed reactor, a radial fixed bed reactor, etc.

[0082] In a preferred embodiment, the supply inlet and discharge outlet of each unit are connected to the supply inlet and discharge outlet of the associated unit via pipelines as required, and preferably have independent valves on each pipeline to regulate the flow rate.

[0083] When used to treat, process, and utilize hydrocarbon-containing mixtures, the present system can achieve efficient and comprehensive utilization of the hydrocarbon-containing mixture and improve the value of the products.

[0084] [Example] The present application is further illustrated by, but not limited to, the following examples.

[0085] (Examples of preparation of aromatic conversion catalysts of the present application) All reagents used in the following preparative examples are commercially available and of reagent grade purity.

[0086] In the following preparation examples, the NH3-TPD pattern of the obtained catalyst was measured by the following method: 100 mg of a sample crushed to 20-40 mesh was weighed, heated to 500°C under nitrogen flow (30 ml / min) at a heating rate of 10°C / min, and purged at a constant temperature for 30 minutes. After the heating treatment was completed, the sample was cooled to 100°C, subjected to ammonia adsorption by introducing NH3 gas, maintained ammonia adsorption for 10 minutes, switched to helium purging (30 ml / min) for 1 hour, and heated to 600°C by temperature programming at a heating rate of 10°C / min. Then, the signal of the NH3 concentration in the effluent was detected by TCD.

[0087] In the following preparation examples, the medium to strong acid content of the catalyst was calculated according to the peak area in the temperature range of 200-400°C in its NH3-TOD pattern; the ratio of the medium to strong acid content to the total acid content of the catalyst was the ratio of the peak area in the temperature range of 200-400°C to the total peak area in the temperature range of 100-600°C in its NH3-TOD pattern.

[0088] In the following preparation examples, the TEM images of the obtained catalysts were characterized by a high-resolution field emission transmission electron microscope, and elemental analysis was performed by an energy scattering X-ray analyzer mounted on the transmission electron microscope at an operating voltage of 200 kV.

[0089] Preparation Example 1 20 g of mordenite was collected and impregnated with a supersaturated ammonium molybdate solution, followed by pre-roasting at 400°C for 3 hours in an air atmosphere to obtain a modified molecular sieve. The modified molecular sieve and 7.7 g of alumina were kneaded and molded, and the resulting product was roasted at 550°C for 2 hours in an air atmosphere to obtain Catalyst A with a molybdenum content of 3 wt%. The composition and properties of the obtained catalyst are shown in Table 1, and the NH3-TPD pattern of the obtained catalyst is shown in Figure 4.

[0090] The TEM electron analysis of the obtained catalyst is shown in Figure 5, where the upper left image shows the TEM phase image of the combination of molecular sieve and alumina, the upper right image shows the distribution of Mo element, the lower left image shows the distribution of silicon element, and the lower right image shows the distribution of aluminum element. From the composition of the obtained catalyst, it can be seen that the silicon-rich part (see lower left image) corresponds to mordenite, while the aluminum-rich part (see lower right image) corresponds to the alumina additive. From the distribution of Mo element (see upper right image), it can be seen that Mo element is mainly distributed on the surface of mordenite in the catalyst.

[0091] Preparation Example 2 20 g of mordenite was collected and impregnated with a supersaturated ammonium perrhenate solution, followed by pre-roasting at 400°C for 3 hours in an air atmosphere to obtain a modified molecular sieve. The modified molecular sieve and 7.7 g of alumina were kneaded to form a powder, and the resulting powder was roasted at 550°C for 2 hours in an air atmosphere to obtain Catalyst B having a rhenium content of 0.5 wt%. The composition and properties of the obtained catalyst are shown in Table 1.

[0092] Preparation Example 3 20 g of mordenite was collected and impregnated with a supersaturated ammonium molybdate solution, followed by pre-roasting at 400°C for 3 hours in an air atmosphere to obtain a modified molecular sieve. The modified molecular sieve and 7.7 g of kaolin were kneaded to form a mold, and the resulting product was roasted at 550°C for 2 hours in an air atmosphere to obtain catalyst C with a molybdenum content of 1 wt%. The composition and properties of the obtained catalyst are shown in Table 1.

[0093] Preparation Example 4 20 g of MCM-22 molecular sieve was collected and supersaturatedly impregnated with ammonium molybdate solution, followed by pre-roasting at 400°C for 3 hours in an air atmosphere to obtain a modified molecular sieve. The modified molecular sieve and 7.7 g of alumina were kneaded to form a mold, and the resulting product was roasted at 550°C for 2 hours in an air atmosphere to obtain Catalyst D, which had a molybdenum content of 3 wt%. The composition and properties of the obtained catalyst are shown in Table 1.

[0094] Preparation Example 5 20 g of MCM-22 was collected and impregnated with a supersaturated ammonium molybdate solution, followed by pre-roasting at 400°C for 3 hours in an air atmosphere. The modified molecular sieve and 7.7 g of alumina were kneaded to form a mold, and the resulting product was roasted at 550°C for 2 hours in an air atmosphere to obtain Catalyst E, which had a molybdenum content of 6 wt%. The composition and properties of the obtained catalyst are shown in Table 1.

[0095] Preparation Example 6 20 g of mordenite was supersaturatedly impregnated with a solution containing ammonium dihydrogen phosphate and ammonium molybdate, and pre-roasted at 400°C for 3 hours in an air atmosphere. The modified molecular sieve and 7.7 g of alumina were kneaded to form a powder, and the resulting powder was roasted at 550°C for 2 hours in an air atmosphere to obtain Catalyst F having 0.5 wt% phosphorus and 3 wt% molybdenum. The composition and properties of the obtained catalyst are shown in Table 1.

[0096] Preparation Example 7 20 g of ZSM-12 was taken and impregnated with a supersaturated ammonium molybdate solution, then pre-roasted at 300°C for 3 hours in an air atmosphere. The modified molecular sieve and 7.7 g of alumina were kneaded to form a mold, and the resultant was roasted at 550°C for 2 hours in an air atmosphere to obtain Catalyst G, which had a molybdenum content of 4 wt%. The composition and properties of the obtained catalyst are shown in Table 1.

[0097] Preparation Example 8 A catalyst was prepared as described in Preparative Example 1 under otherwise identical conditions, except that a certain amount of mordenite was taken and impregnated with a solution of ammonium molybdate and ammonium tungstate, to obtain a catalyst with a Mo content of 1.5 wt % and a W content of 1.5 wt %. The composition and properties of the obtained catalyst are shown in Table 1.

[0098] Preparation Example 9 A catalyst was prepared as described in Preparative Example 1 under otherwise identical conditions, except that a specific amount of mordenite was impregnated with a specific amount of ammonium molybdate, ammonium tungstate, and ammonium perrhenate solution, resulting in a catalyst with a Mo content of 2 wt %, a W content of 0.4 wt %, and a Re content of 0.6 wt %. The composition and properties of the resulting catalyst are shown in Table 1.

[0099] Preparation Example 10 A catalyst was prepared as described in Preparation Example 1, except that a certain amount of mordenite was impregnated with an ammonium molybdate solution to obtain a modified molecular sieve powder, and the modified molecular sieve was pre-roasted at 400°C for 3 hours under a mixed atmosphere of air and steam (air to steam volume ratio 20:1). Other conditions for preparing the catalyst were the same to obtain Catalyst J. Its composition and properties are shown in Table 1.

[0100] Preparation Example 11 A catalyst was prepared as described in Preparation Example 1, except that a certain amount of mordenite was impregnated with an ammonium molybdate solution to obtain a modified molecular sieve powder, and the modified molecular sieve was roasted at 400°C for 3 hours under a mixed atmosphere of air and steam (air and steam volume ratio 5:1). Other conditions for preparing the catalyst to obtain Catalyst M were the same. The composition and properties of the obtained catalyst are shown in Table 1.

[0101] Preparation Example 12 A catalyst was prepared as described in Preparative Example 1, except that a certain amount of mordenite was impregnated with an ammonium molybdate solution to obtain a modified molecular sieve powder, which was then dried at 120°C to obtain a modified molecular sieve. 20 g of the modified molecular sieve and 7.7 g of alumina were kneaded together to form a shape, and the resultant was roasted at 550°C for 2 hours to obtain Catalyst N. The composition and properties of the obtained catalyst are shown in Table 1.

[0102] Preparation Example 13 A specific amount of mordenite was impregnated with a solution of specific amounts of ammonium molybdate, ammonium tungstate, and ammonium perrhenate to obtain a modified molecular sieve, which was then pre-roasted at 400°C for 3 hours in a mixed atmosphere of air and steam (air to steam volume ratio: 20:1), except that the modified molecular sieve was prepared under the same conditions as in Preparation Example 9 to obtain Catalyst O. The composition and properties of the obtained catalyst are shown in Table 1.

[0103] [Table 1]

[0104] (Example of a method for treating a hydrocarbon-containing mixture) The following Examples 1-3 illustrate the practice of the present process using a conventional catalyst: Aromatization catalyst: Zn and Mo modified ZSM-5 molecular sieve, having a Zn content (calculated as the metal element) of 5 wt.%, a Mo content (calculated as the metal element) of 2 wt.%, a ZSM-5 molecular sieve content of 70 wt.%, and the remainder being alumina; Aromatic conversion catalyst: Re-modified MOR zeolite with a Re content (calculated as the metal element) of 0.5 wt. %, a mordenite content of 70 wt. %, and the remainder being alumina; Hydrogenation saturated catalyst: a catalyst containing Pt and Ni supported on an alumina support, in which the Pt content is 0.1 wt %, the Ni content (calculated as metal element) is 8 wt %, and the rest is an alumina support; Non-aromatic cracking catalyst: A catalyst comprising a ZSM-5 / β molecular sieve mixture and Mo supported on the mixture, wherein the ZSM-5 molecular sieve content is 60 wt%, the β molecular sieve content is 34 wt%, and the Mo content (calculated as the metallic element) is 6 wt%.

[0105] Unless otherwise specified, each catalyst used was prepared by conventional methods known in the art.

[0106] Example 1 Referring to the flow chart shown in Example 1, 100 tons / hour of catalytic cracking gasoline is subjected to pre-treatment for desulfurization and denitrification, and then passed through an aromatics fractionation column to separate C7 - Light fractions of C8 + The heavy fraction was separated into C7 and C8. - The light fraction of C5 in the resulting product is sent to the aromatization unit. - light hydrocarbons as cracking feedstock, and C6 in the resulting product for further conversion. + The components were sent to the aromatics conversion unit. C8 +The heavy fraction is sent to the aromatic conversion unit to carry out reactions such as aromatic transalkylation and non-aromatic hydrocracking, and the resulting C8 components are sent to the aromatic extraction unit for purification, and the resulting by-product C5 - The light fraction was recovered and used as cracking feedstock, and the remaining unreacted components were recycled to the aromatics conversion unit. The C8 aromatic hydrocarbons obtained by aromatics extraction were recovered as products, with a purity of 99.8%, and the remaining non-aromatic hydrocarbons were used as cracking feedstock.

[0107] The feedstock composition, reaction conditions for each unit, and product yields for the integrated units are shown in Tables 2, 3, and 4, respectively.

[0108] Example 2 Referring to the flow chart shown in Figure 2, 100 tonnes / hour of a mixture of catalytic cracking gasoline and thermal cracking gasoline is subjected to desulfurization and denitrification, and then passed through an aromatics fractionation column to separate C5 - light fraction and C6 + The heavy fraction was separated into C5 - The light fraction of C5 in the product obtained after hydrogenation saturation is sent to the aromatization unit. - The components are used as cracking feedstocks to obtain C6 in the resulting products for further conversion. + The components were sent to the aromatics conversion unit. + The heavy fraction is sent to the aromatic conversion unit to carry out the transalkylation reaction and the non-aromatic mild hydrocracking reaction, and the resulting C8 components are sent to the non-aromatic cracking unit for further purification, and the resulting by-product C5 - The light fraction of the non-aromatic hydrocarbons was used as the cracking feedstock, and the remaining unreacted components were recycled to the aromatics conversion unit. The non-aromatic hydrocarbons were subjected to selective cracking in the non-aromatic hydrocarbon cracking unit, and the resulting C8 aromatic hydrocarbons were recovered as the product, with a purity of 99.9%. The light hydrocarbons (i.e., non-aromatic components) obtained as by-products of the non-aromatic hydrocarbon cracking unit were recovered as the cracking feedstock.

[0109] The feedstock composition, reaction conditions for each unit, and product yields for the integrated units are shown in Tables 2, 3, and 4, respectively.

[0110] Example 3 Referring to the flow chart shown in FIG. 3, 100 tonnes / hour of a mixture of catalytic cracking gasoline and thermal cracking gasoline is desulfurized and denitrified, and then passed through an atmospheric rectification column to produce C5 - light fraction and C6 + The heavy fraction was separated into C5 - The light fraction of C5 in the product obtained after hydrogenation saturation is sent to the aromatization unit. - The components are used as cracking feedstocks to further convert C6 + The components were sent to the aromatics conversion unit. + The heavy fraction is sent to the aromatic conversion unit to carry out the transalkylation reaction and the non-aromatic mild hydrocracking reaction, and the resulting C8 components are sent to the non-aromatic cracking unit for further purification, and the resulting by-product C5 - The light fraction of the non-aromatic hydrocarbons was used as the cracking feedstock, and the remaining unreacted components were recycled to the aromatics conversion unit. The non-aromatic hydrocarbons were subjected to selective cracking in the non-aromatic hydrocarbon cracking unit, and the resulting C8 aromatic hydrocarbons were recovered as the product, with a purity of 99.9%. After hydrogenation saturation, the light hydrocarbons obtained as the by-products of the non-aromatic hydrocarbon cracking unit were recovered as the cracking feedstock.

[0111] The feedstock composition, reaction conditions for each unit, and product yields for the integrated units are shown in Tables 2, 3, and 4, respectively.

[0112] [Table 2]

[0113] [Table 3] JPEG0007742404000004.jpg136169

[0114] [Table 4]

[0115] As can be seen from the test results in Table 4, the processing method of the present application can be flexibly used to process various hydrocarbon-containing mixtures, and the resulting products mainly include C8 aromatic hydrocarbons, ethylene, and propylene, with a total yield of 85% or more. In a preferred embodiment, the total yield (C8 aromatic hydrocarbons + ethylene + propylene) can reach 92%.

[0116] The following Examples 4-17 illustrate the practice of the present process using the present aromatic conversion catalyst.

[0117] Examples 4 to 16 Before use, catalysts A to O obtained in Preparation Examples 1 to 13 were separated in a reactor and reduced by introducing hydrogen gas at 450°C for 3 hours. Then, gasoline feedstock was treated in the same manner as in Example 1 under the same operating conditions, except that the aromatic conversion catalyst used in Example 1 was replaced with catalysts A to O. The results are shown in Table 5.

[0118] Example 17 The steam cracking unit was replaced with a catalytic cracking unit (i.e., a fluidized bed reactor), and the reaction temperature was 500°C and the weight hourly space velocity was 5 h -1 The gasoline feed was treated as described in Example 16, with other operating conditions being the same, except that the catalyst to oil ratio was 1 and the pressure was 0.2 MPa. The results are shown in Table 5.

[0119] [Table 5] JPEG0007742404000007.jpg160169

[0120] As can be seen from the test results in Table 5, by using the aromatics conversion catalyst of the present application, the yield of C8 aromatic hydrocarbons can be further increased, and in a preferred embodiment, the total yield (C8 aromatic hydrocarbons + ethylene + propylene) can be further increased to 93 wt % or more.

[0121] Although the present application has been described in detail above with reference to preferred embodiments, it is not intended to be limited to these embodiments. Various modifications may be made in accordance with the inventive concept of the present application, and these modifications must be made within the scope of the present application.

[0122] It should be noted that the various technical features described in the above embodiments may be combined in any suitable manner without contradiction, and in order to avoid unnecessary repetition, the present application does not describe various possible combinations, but such combinations are also intended to fall within the scope of the present application.

[0123] Furthermore, various embodiments of the present application may be combined in any manner unless such combination deviates from the spirit of the present application, and such combined embodiments should be considered as part of the disclosure of the present application. [Brief explanation of the drawings]

[0124] [Figure 1] FIG. 1 is a schematic flow diagram of a preferred embodiment of the method according to the present application. [Figure 2] FIG. 2 is a schematic flow diagram of another preferred embodiment of the method according to the present application. [Figure 3] FIG. 3 is a schematic flow diagram of another preferred embodiment of the method according to the present application. [Figure 4] FIG. 4 shows the NH3-TPD pattern of the catalyst obtained in Preparation Example 1 of the present application. [Figure 5] FIG. 5 shows a TEM image of the catalyst obtained in Preparation Example 1 of the present application.

Claims

1. A method for treating a hydrocarbon-containing mixture, comprising the steps of: I) separating the hydrocarbon-containing mixture into a light fraction and a heavy fraction, wherein the light fraction is C ７ － component, and the heavy fraction is C ８ ＋ or the light fraction is C ５ － component, and the heavy fraction is C ６ ＋ It is an ingredient; II) in an aromatization unit, reacting the light fraction from step I) in the presence of an aromatization catalyst to obtain a reaction product of C ５ － Ingredients and C ６ ＋ wherein the reaction occurring in the aromatization unit comprises an aromatization reaction; III) in an aromatics conversion unit, the heavy fraction from step I) and optionally the C from step II) are treated in the presence of an aromatics conversion catalyst; ６ ＋ The components are reacted to form a reaction product, ５ － Ingredients and C ６ ~C ７ Ingredients and C ８ Ingredients and C ９ ＋ wherein the reaction occurring in the aromatic conversion unit comprises a transalkylation reaction; IV) the C from step II) ５ － component and said C from step III) ５ － catalytically cracking at least a portion of one or both of the components or subjecting it to steam cracking after optional hydrosaturation; V) the C from step III) ８ The components are purified and ８ Aromatic hydrocarbons and non-aromatic components are obtained, and at least a portion of the obtained non-aromatic components is treated with the C ５ － dissolving together the components; and VI) the C from step III) ６ ~C ７ Component and the C ９ ＋ recycling at least a portion of one or more of the components to said aromatic conversion unit of step III) for further reaction.

2. 10. The method of claim 1, wherein the hydrocarbon-containing mixture comprises C3 to C12 hydrocarbons and has a distillation range of 40 to 300°C.

3. 3. The method of claim 1 or 2, wherein the hydrocarbon-containing mixture is selected from catalytic diesel or its hydrogenation products, catalytic cracking gasoline, hydrocracked gasoline, ethylene cracking gasoline, straight run naphtha, catalytic reformate, LPG, or any mixture thereof.

4. 3. The method of claim 1 or 2, wherein the aromatization catalyst used in the aromatization unit of step II) comprises 50 to 90 wt. % of a molecular sieve selected from aluminosilicates, aluminogallosilicates, aluminosilicophosphates, aluminoferrosilicates, or combinations thereof, having a pore structure of 10 or 12 ring members, and 0.5 to 10 wt. % of a modifying metal selected from the group consisting of Group IB metals, Group IIB metals, Group VIB metals, Group VIIB metals, and Group VIII metals.

5. The reaction conditions for step II) are a reaction temperature of 400 to 600°C, a reaction pressure of 0.2 to 3 MPa, and a reaction time of 0.5 to 5 hours. －１ 3. The method of claim 1 or 2, comprising a feed weight hourly space velocity of

6. 3. The method of claim 1, wherein the aromatic conversion catalyst comprises a molecular sieve component, an active metal component fixed on the molecular sieve component, and an oxide additive, the catalyst having a medium-to-strong acid content of 0.05 to 2.0 mmol / g catalyst, and the ratio of the medium-to-strong acid content to the total acid content is 60 to 99%, the molecular sieve component being selected from the group consisting of MCM-22 molecular sieve, MOR molecular sieve, ZSM-12 molecular sieve, and combinations thereof; the active metal in the active metal component being selected from the group consisting of Group VB metals, Group VIB metals, Group VIIB metals, and combinations thereof; and the oxide additive being selected from the group consisting of alumina, silica, magnesia, titania, zirconia, kaolin, and combinations thereof.

7. 7. The method of claim 6, wherein the aromatic conversion catalyst comprises 50 to 90 wt. % of the molecular sieve component, 5 to 40 wt. % of the oxide additive, and 0.01 to 10 wt. % of the active metal component, based on the total weight of the catalyst.

8. 8. The method of claim 7, wherein the aromatic conversion catalyst further comprises a phosphorus-containing component immobilized on the molecular sieve component.

9. P ２ O ５ 9. The process of claim 8, wherein the phosphorus content, calculated as:

10. 8. The method of claim 7, wherein the active metal is present in the aromatic conversion catalyst in the form of an elemental metal, a metal oxide, or a combination thereof, and is one or more of Mo, W, and Re.

11. 11. The method according to claim 10, wherein the active metal is a combination of two of Mo, Re, and W, wherein the weight ratio of the mixture, calculated as metal elements, is 0.1 to 10:1, or the active metal is a combination of Mo, Re, and W, wherein the weight ratio of Mo, Re, and W, calculated as metal elements, is 1:0.1 to 0.4:0.1 to 0.

6.

12. The reaction conditions for step III) are a reaction temperature of 250 to 500°C, a reaction pressure of 1.5 to 6.5 MPa, a molar ratio of hydrogen to hydrocarbon of 1 to 10, and a reaction time of 0.5 to 5 hours. －１ 3. The method of claim 1 or 2, comprising a feed weight hourly space velocity of

13. 3. The method of claim 1 or 2, wherein the hydrosaturation in step IV) is carried out in the presence of a catalyst comprising a metal component selected from the group consisting of Ni, Mo, Co, Pt, Pd, and combinations thereof, and a support component selected from the group consisting of alumina, kaolin, magnesia, silica, titania, calcium oxide, amorphous silica-alumina, and combinations thereof.

14. The operating conditions for hydrogenation saturation are a reaction temperature of 150 to 600°C, a reaction pressure of 0.5 to 6 MPa, and a reaction time of 0.5 to 10 hours. －１ and a volume ratio of hydrogen to hydrocarbon of 200 to 2000.

15. The operating conditions for steam cracking in step IV) include a cracking temperature of 600 to 1000°C, a residence time of 0.01 to 0.8 seconds, and a reaction pressure of 0.1 to 0.3 MPa; or The operating conditions for catalytic decomposition in step IV) are a reaction temperature of 450-650°C, a reaction time of 0.5-20 hours －１ 3. The method according to claim 1 or 2, comprising a weight hourly space velocity of 0.05 to 0.5 MPa, a reaction pressure of 0.05 to 0.5 MPa, and a mass ratio of catalyst to oil of 0.1 to 10.

16. The purification step of step V) is ８ 3. The method of claim 1 or 2, comprising subjecting the components to aromatic extractive separation, non-aromatics selective cracking, or a combination thereof.

17. The purification step is ８ subjecting the components to extractive separation via extractive distillation using sulfolane solvent; or The purification step is ８ subjecting the components to non-aromatic selective cracking in the presence of a catalyst comprising a molecular sieve selected from the group consisting of ZSM-5 molecular sieve, MCM-22 molecular sieve, MOR molecular sieve, β molecular sieve, and combinations thereof, and optionally a metal component selected from Group VIB metals, Group VIIB metals, and Group VIII metals; wherein the operating conditions for the non-aromatic selective cracking are a reaction temperature of 300 to 600°C, a reaction pressure of 0.5 to 3.0 MPa, a molar ratio of hydrogen to hydrocarbon of 1 to 10, and a reaction time of 1 to 15 hours. －１ 17. The method of claim 16, wherein the weight hourly space velocity is

18. a separation unit for separating the hydrocarbon-containing mixture into the light fraction and the heavy fraction; The light fraction from the separation unit is reacted and the resulting reaction product is separated to obtain C ５ － Ingredients and C ６ ＋ an aromatization unit for obtaining components; the heavy fraction from the separation unit, and optionally the C from the aromatization unit. ６ ＋ The components are reacted and the resulting reaction product is separated to form C ５ － Ingredients, C ６ ~C ７ Ingredients, C ８ Component C ９ ＋ an aromatics conversion unit to obtain components; The C from the aromatization unit ５ － component and the C from the aromatic conversion unit. ５ － a cracking unit for catalytically cracking at least a portion of one or both of the components or subjecting it to steam cracking after optional hydrosaturation; Optionally, the C from the aromatization unit ５ － component and the C from the aromatic conversion unit. ５ － a hydrogenation saturation unit for hydrogenating at least a portion of one or both of the components to saturation; and The C from the aromatic conversion unit ８ The components are purified and ８ an aromatics refining unit for obtaining aromatic hydrocarbons and non-aromatic components; Including, wherein the aromatic conversion unit comprises an inlet, a C 5 − component outlet, a C 6 to C 7 component outlet, a C 8 component outlet, and a C 9 + component outlet; the decomposition unit having an inlet and a decomposition product outlet; A system for carrying out the method for treating a hydrocarbon-containing mixture according to any one of claims 1 to 17, wherein the aromatic purification unit comprises an inlet, a C8 aromatic hydrocarbon outlet, and a non-aromatic component outlet, the C8 component outlet of the aromatic conversion unit being in communication with the inlet of the aromatic purification unit, and the non-aromatic component outlet of the aromatic purification unit being in communication with the inlet of the cracking unit, optionally through the hydrosaturation unit.

19. the separation unit comprising a hydrocarbon-containing mixture inlet, a light ends outlet, and a heavy ends outlet; The aromatization unit comprises an inlet, a ５ － Component outlet, and C ６ ＋ having a component outlet; wherein the light fraction outlet of the separation unit is in communication with the inlet of the aromatization unit, the heavy fraction outlet of the separation unit is in communication with the inlet of the aromatic conversion unit, and the C ５ － The component outlet and the C of the aromatic conversion unit ５ － 20. The system of claim 18, wherein one or both of the component outlets are in communication with the inlet of the cracking unit, optionally through the hydrosaturation unit.

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