System and method for producing olefins and / or aromatics by first low and medium water treatment followed by high water treatment and steam cracking

Abstract

Disclosed herein are systems and methods for producing olefins and / or aromatics. These processes include treatment before and after two-stage water treatment of crude oil and / or heavy oil in a steam cracking unit to produce olefins and / or aromatics. The first-stage water treatment and the second-stage water treatment are operated at different intensities. The system comprises two water treatment units which can operate under different intensities.

Description

CROSS-REFERENCE TO RELATED APPLICATIONS

[0001] none. background A. Technical field

[0002] The present invention generally relates to the production of olefins and / or aromatics. More specifically, the present invention relates to the production of olefins and / or aromatics from crude oil and / or heavy oil by two-stage water treatment and steam cracking. B. Background Technology

[0003] In the process of processing crude oil to produce olefins and aromatics, slurry and ebullated-bed hydrocracking units are used to convert bottom-of-the-barrel crude oil (i.e., the crude oil fraction with the highest boiling point in crude oil). Light crude oil fractions in the vacuum gas oil range are separately sent through fixed-bed hydrocracking units. The investment in crude oil chemical plants is very high, at least in part due to the high cost of steam crackers and hydrocracking units. High conversion rates of crude oil streams can lead to coke accumulation in fixed-bed hydrocrackers, which shorten the fluidization time. On the other hand, slurry and ebullated-bed reactors that can handle coke are more expensive. Summary of the invention

[0004] The inventors have found a method to solve one or more of the above problems. According to an embodiment of the present invention, the solution includes two-stage water treatment of crude oil and / or heavy ends, followed by cracking, thereby producing olefins and / or aromatics. According to an embodiment of the present invention, the cost of a fixed bed water treatment device is lower than that of a slurry reactor, so it is advantageous for most of the water flow to pass through a fixed bed water treatment device, while only a portion of the water flow passes through a more expensive slurry / ebullating bed reactor. In an embodiment of the present invention, in addition to conventional crude oil feeds, or as a substitute for conventional crude oil feeds, plastics, plastic pyrolysis oligomers, synthetic crude oils and / or hydrocarbon streams produced by plastic pyrolysis can also be co-processed. In addition, in an embodiment of the present invention, bio-oil can be co-processed with crude oil, or as a substitute for crude oil.

[0005] Embodiments of the present invention include a method for producing olefins and / or aromatics. The method includes flowing a hydrocarbon feed into a first water treatment unit, a first catalyst is disposed in the first water treatment unit, and the hydrocarbon feed is water treated in the first water treatment unit to produce a first top stream having a boiling point below 200°C and a first bottom stream, the first bottom stream comprising diesel and / or fuel oil, and a boiling point between 305°C and 650°C. The water treatment of the hydrocarbon feed includes contacting the hydrocarbon feed with the first catalyst in a temperature range of 280 to 400°C. The method also includes flowing the first bottom stream into a second water treatment unit, a second catalyst is disposed in the second water treatment unit, and the first bottom stream is water treated in the second water treatment unit to produce a second top stream having a boiling point below 305°C and a second bottom stream, the second bottom stream comprising one or more of asphalt, coke and fuel oil, and a boiling point between 305°C and 650°C. The water treatment of the first bottom stream includes contacting the first bottom stream with the catalyst in a temperature range of 400 to 500°C. The method also includes treating the second overhead stream in a steam cracker to produce olefins and / or aromatics. The water treatment is to hydrocracking the hydrocarbons in the presence of (a) one or more catalysts and (b) a solvent that keeps the asphaltenes dissolved at a temperature of 280 to 550° C. and a pressure range of 40 to 200 barg. In an embodiment of the present invention, the water treatment conditions may include a liquid feed with a hydrogen to hydrocarbon ratio of 200 to 2000 NL / L, and the water treatment may be performed with or without the addition of steam.

[0006] Embodiments of the present invention include a system for producing olefins and / or aromatics. The system includes a first water treatment unit, in which a first catalyst is provided, for contacting hydrocarbons with the first catalyst in a temperature range of 280 to 400°C, and producing a first top stream with a boiling point of up to 200°C and a first bottom stream with a boiling point of 305 to 650°C, the first bottom stream comprising diesel and / or fuel oil. The system also includes a second water treatment unit, in which a second catalyst is provided, and the first bottom stream is fluidly connected to the first water treatment unit. The second water treatment unit is used to contact the first bottom stream with a second catalyst in a temperature range of 400 to 500°C, and produce a second top stream with a boiling point below 305°C and a second bottom stream composed of one or more of asphalt, coke or fuel oil and having a boiling point in the range of 305 to 650°C. The system also includes a steam cracking unit in fluid communication with the first water treatment unit and the second water treatment unit. The steam cracking unit is used to produce olefins and / or aromatics from the first top stream and the second top stream.

[0007] Included below are definitions of various terms and phrases used throughout this specification.

[0008] The term "about" or "approximately" is defined as close to the degree understood by those of ordinary skill in the art. In a non-limiting embodiment, these terms are defined as within 10%, preferably within 5%, more preferably within 1%, and most preferably within 0.5%.

[0009] For the purposes of this disclosure, “X, Y, and / or Z” may be understood as only X, only Y, only Z, or any combination of two or more items X, Y, and Z (e.g., XYZ, XY, XZ, YZ).

[0010] The terms "wt. %, "vol. %" or "mol. %" refer to the weight, volume or mole percentage based on the total weight, total volume or total moles of the material containing the component, respectively. In a non-limiting example, 100 moles of a material containing 10 moles of a component is 10 mol. % of the component.

[0011] The term "substantially" and variations thereof are defined to include ranges within 10%, within 5%, within 1%, or within 0.5%.

[0012] The terms "inhibit" or "reduce" or "prevent" or "avoid" or any variation of these terms as used in the claims and / or description include any measurable reduction or complete inhibition to achieve the desired result.

[0013] The term "effective" as used in the specification and / or claims means sufficient to achieve an intended, desired, or purposeful result.

[0014] The words "a" or "an" used in conjunction with the terms "comprising," "including," "containing," or "having" in the claims or specification may mean "one," but are also consistent with the meaning of "one or more," "at least one," and "one or more."

[0015] The words "comprise" (and any form of inclusion, such as "include" and "contain"), "have" (and any form of having, such as "have" and "contain"), "include" (and any form of inclusion, such as "includes" and "have"), or "contains" (and any form of containing, such as "including" and "including") are inclusive or open-ended and do not exclude additional, unrecited elements or method steps.

[0016] The processes of the present invention may "comprise," "consist essentially of," or "consist of" the particular ingredients, components, compositions, etc. disclosed throughout the specification.

[0017] The term "mainly" used in the specification and / or claims refers to any one of greater than 50 wt.%, 50 mol.%, and 50 vol.%. For example, "mainly" may include 50.1 wt.% to 100 wt.% and all values ​​and ranges therebetween, 50.1 mol.% to 100 mol.% and all values ​​and ranges therebetween, or 50.1 vol.% to 100 vol.% and all values ​​and ranges therebetween.

[0018] Other objects, features and advantages of the present invention will be apparent from the following figures, detailed descriptions and examples. However, it should be understood that these figures, detailed descriptions and examples, although indicating specific embodiments of the present invention, are for illustrative purposes only and are not intended to be limiting. In addition, changes and modifications within the spirit and scope of the present invention will also be apparent to those skilled in the art. In more embodiments, the features of a particular embodiment may be combined with the features of other embodiments. For example, the features of one embodiment may be combined with the features of any other embodiment. In more embodiments, other features may also be added to the specific embodiments described herein. BRIEF DESCRIPTION OF THE DRAWINGS

[0019] For a more complete understanding, reference is now made to the following description taken in conjunction with the accompanying drawings, in which:

[0020] Figure 1 A system for producing olefins and / or aromatics according to an embodiment of the present invention is shown; and

[0021] Figure 2 A method for producing olefins and / or aromatics according to an embodiment of the present invention is shown. DETAILED DESCRIPTION

[0022] The embodiment of the present invention relates to an enhanced upgrading process for the heavy end of crude oil - a water treatment process. This water treatment process can replace multiple conventional hydrocracking units in a crude oil chemical plant. According to an embodiment of the present invention, water treatment is carried out in two stages. In an embodiment of the present invention, the first stage is carried out in a first water treatment unit operated at a low or medium degree to avoid coking and pressure drop problems that occur in fixed bed units and in processes with longer flow times. According to an embodiment of the present invention, the heavier products cut from the first stage are converted in the second stage, and the second stage is carried out by a second water treatment unit, which operates under more severe conditions than the first water treatment unit. In an embodiment of the present invention, the second water treatment unit includes one or more boiling / slurry reactors, and more severe conditions can maximize the conversion rate and avoid pressure drop problems caused by higher conversion rates. According to an embodiment of the present invention, products from the first water treatment unit and the second water treatment unit are converted into high-value chemicals such as olefins and / or aromatics in a steam cracking unit.

[0023] Figure 1 A system 10 for producing olefins and / or aromatics according to an embodiment of the present invention is shown. Figure 2 A method 20 for producing olefins and / or aromatics according to an embodiment of the present invention is shown. In an embodiment of the present invention, the method 20 is implemented using the system 10. Systems for producing olefins and / or aromatics

[0024] Figure 1 A separation unit 103 (e.g., a flash vessel, a distillation column, and / or a stripping unit) is shown, which in embodiments of the present invention is suitable for separating (a) crude oil 100 and / or (b) a first heavy oil stream 101, the first heavy oil stream 101 comprising any combination of crude oil, plastic, hydrocarbons produced by pyrolysis of plastic, bio-oil, hydrogenated bio-oil, oligomers produced by plastic, synthetic crude oil and pyrolysis oil derived from plastic, bottom cut of crude oil cut, pyrolysis oil and heavy residue from a steam cracker (wherein (a) and (b) form a combined feed stream 102) to produce (1) an upper crude oil cut stream 104 having a boiling point range not exceeding 200°C and (2) a lower crude oil cut stream 105 having a boiling point greater than 200°C. In embodiments of the present invention, the separation unit 103 may include one or more of the following: a flash vessel, a distillation column, and / or a stripping unit. According to embodiments of the present invention, the system 10 includes a first water treatment unit 109, which includes a first reactor unit 110 and a first separation unit 112. In an embodiment of the present invention, the first water treatment unit 109 is used to receive the hydrogen gas stream 107 and the hydrocarbon feed 108. In an embodiment of the present invention, the hydrocarbon feed 108 includes the bottom crude oil cut stream 105 and the second heavy oil stream 106, the circulating pyrolysis oil from the steam cracking furnace, and optional water. According to an embodiment of the present invention, the first reactor device 110 is used to receive the hydrocarbon feed 108 and the hydrogen gas stream 107. In an embodiment of the present invention, the first reactor unit 110 includes a fixed bed reactor, in which a first catalyst is disposed, and is suitable for contacting the hydrogen gas stream 107 and the hydrocarbon feed 108 with the first catalyst in a temperature range of 280 to 400° C. to produce a first reactor unit effluent 111. In an embodiment of the present invention, the first separation unit 112 includes one or more distillation columns for receiving and separating the first reactor unit effluent 111 to produce a first top stream 113, an intermediate stream 114, and a first bottom stream 115. According to an embodiment of the present invention, the boiling point range of the first top stream 113 is up to 200°C, the boiling point range of the intermediate stream 114 is 200 to 305°C, and the first bottom stream 115 contains diesel and / or fuel oil with a boiling point range of 305 to 650°C.

[0025] According to an embodiment of the present invention, the system 10 further includes a second water treatment unit 116, which includes a second reactor unit 117 and a second separation unit 119. According to an embodiment of the present invention, the second reactor unit 117 is in fluid communication with the first water treatment unit 109 and is suitable for receiving the first bottom stream 115. In an embodiment of the present invention, the second reactor unit 117 includes a boiling reactor and / or a slurry reactor, in which a second catalyst is configured, and is suitable for contacting the first bottom stream 115 with the second catalyst at a temperature range of 400 to 500° C. to produce a second reactor unit effluent 118. In an embodiment of the present invention, the second separation unit 119 includes one or more distillation columns, which are suitable for receiving and separating the second reactor unit effluent 118 to produce a second top stream 120 and a second bottom stream 121. According to an embodiment of the present invention, the second top stream 120 has a boiling point range of up to 305° C., and the second bottom stream 121 includes one or more of asphalt, coke or fuel oil, with a boiling point range of 305° C. to 650° C.

[0026] In an embodiment of the present invention, the system 10 includes a steam cracking unit 122 that is fluidly connected to the separation unit 103, the first water treatment unit 109 and the second water treatment unit 116, so that the top crude oil cut liquid stream 104, the first top material stream 113, the intermediate material stream 114 and / or the second top material stream 120 can flow to the steam cracking unit 122 for processing to produce a high-value chemical liquid stream 123 including olefins and / or aromatics. Process for producing olefins and / or aromatics

[0027] Figure 2A method 20 according to an embodiment of the present invention is shown, including block 200, which involves feeding (a) crude oil 100 and / or (b) a first heavy oil stream 101 (including any combination of crude oil, plastic, hydrocarbons produced by pyrolysis of plastic, bio-oil, hydrogenated bio-oil, oligomers produced by plastic, pyrolysis oil produced by synthetic crude oil and plastic, bottom cuts of crude oil cuts, pyrolysis oil, and heavy residues produced by steam cracking furnaces) into a separation unit 103 (wherein (a) and (b) form a combined feed stream 102). At block 201, according to an embodiment of the present invention, the separation unit 103 separates (a) crude oil 100 and / or (b) the first heavy oil stream 101 to produce (1) a top crude oil cut stream 104 having a boiling point in the range below 200°C and (2) a bottom crude oil cut stream 105 having a boiling point above 200°C. At block 202, in an embodiment of the present invention, the method 20 includes conveying the bottom crude oil cut stream 105 and / or the second heavy oil stream 106 to a first water treatment unit 109. In an embodiment of the present invention, the bottom crude oil cutting stream 105 and / or the second heavy oil stream 106 are combined to form a hydrocarbon feed 108. In an embodiment of the present invention, at block 203, the hydrogen stream 107 and the hydrocarbon feed 108, water and the circulating pyrolysis oil from the steam cracking device flow to the first reactor unit 110. In section 204, according to an embodiment of the present invention, the first reactor unit 110 includes a fixed bed reactor, and a first catalyst (for example, a commercial catalyst for fixed bed hydrocracking with high activity: a catalyst including one or more of the following: an organic metal compound having one or more of Ni, Mo, Co, W, Zr; NiMo; NiCoMo; NiMoW; alumina and zeolite) is arranged therein for contacting the hydrocarbon feed 108 and the hydrogen stream 107 (optionally water and the circulating pyrolysis oil from the steam cracking furnace) with the first catalyst at a temperature range of 280 to 400°C to produce a first reactor unit effluent 111. In an embodiment of the present invention, at block 205, the first reactor unit effluent 111 flows to the first separation unit 112. At block 206, in an embodiment of the present invention, the first separation unit 112 (which may include one or more distillation columns) receives and separates the first reactor unit effluent 111 to produce a first overhead stream 113, an intermediate stream 114, and a first bottom stream 115. According to an embodiment of the present invention, the first overhead stream 113 has a boiling point range of up to 200°C, the intermediate stream 114 has a boiling point range of 200 to 305°C, and the first bottom stream 115 contains diesel and / or fuel oil with a boiling point range of 305 to 650°C.

[0028] According to an embodiment of the present invention, the method 20 further includes, at block 207, flowing the first bottom stream 115 into a second water treatment unit 116, the second water treatment unit 116 including a second reactor unit 117 and a second separation unit 119. At block 208, according to an embodiment of the present invention, the second reactor unit 117 includes a boiling reactor and / or a slurry reactor, and a second catalyst (e.g., a commercial catalyst for fixed-bed hydrocracking with high activity: a catalyst including one or more of the following: an organic metal compound having one or more of Ni, Mo, Co, W, Zr; NiMo; NiCoMo; NiMoW; alumina and zeolite) is arranged therein for contacting the first bottom stream 115 with hydrogen, optionally water and circulating pyrolysis oil from a steam cracking furnace with the second catalyst at a temperature range of 400 to 500° C. to produce a second reactor unit effluent 118. In an embodiment of the present invention, at block 209, the second reactor unit effluent 118 flows to the second separation unit 119. In section 210, according to an embodiment of the present invention, a second separation unit 119 (which may include one or more distillation columns) receives and separates the second reactor unit effluent 118 to produce a second top stream 120 and a second bottom stream 121. According to an embodiment of the present invention, the second top stream 120 has a boiling point below 305°C, and the second bottom stream 121 includes one or more of asphalt, coke, or fuel oil, with a boiling point between 305°C and 650°C.

[0029] In an embodiment of the present invention, method 20 includes passing the top crude cut stream 104, the first top stream 113, the intermediate stream 114, and / or the second top stream 120 to a steam cracking unit 122 at block 211. At block 212, embodiments of the present invention include steam cracking unit 122 processing the top crude cut stream 104, the first top stream 113, the intermediate stream 114, and / or the second top stream 120 to produce a high-value chemical stream 123, including olefins and / or aromatics. In embodiments of the present invention, olefins produced at block 212 include ethylene, propylene, butenes, and butadiene, and aromatics include benzene, toluene, xylenes, and ethylbenzene.

[0030] Although the embodiments of the present invention have been described with reference to Figure 2 However, it should be understood that the operation of the present invention is not limited to Figure 2 Therefore, embodiments of the present invention may use different Figure 2 The various blocks in the order described herein are used to provide the functions described in this document.

[0031] The systems and processes described herein may also include various devices not shown, which are known to those skilled in the art of chemical processing. For example, certain controllers, pipelines, computers, valves, pumps, heaters, thermocouples, pressure indicators, mixers, heat exchangers, etc. may not be shown.

[0032] In terms of the present invention, at least the following 23 embodiments are disclosed. Embodiment 1 is a method for producing olefins and / or aromatics. The method comprises flowing a hydrocarbon feed and hydrogen, as well as optional water and circulating pyrolysis oil from a steam cracking furnace, into a first water treatment unit in which a first catalyst is disposed. The method also comprises water-treating the hydrocarbon feed in the first water treatment unit to produce a first top stream having a boiling point in the range of up to 200°C and a first bottom stream comprising diesel and / or fuel oil and having a boiling point in the range of 305 to 650°C, wherein the water treatment of the hydrocarbon feed comprises contacting the hydrocarbon feed and hydrogen with a first catalyst at a temperature in the range of 280 to 400°C. The method further comprises flowing the first bottom stream into a second water treatment device in which a second catalyst is disposed. In addition, the method also includes water treating the first bottom stream with hydrogen, optionally water and circulating pyrolysis oil in a second water treatment unit to produce a second top stream having a boiling point in the range of up to 305°C, and a second bottom stream comprising one or more of asphalt, coke or fuel oil, with a boiling point in the range of 305 to 650°C, wherein the water treatment of the first bottom stream includes contacting the first bottom stream with a second catalyst at a temperature in the range of 400 to 500°C. The method also includes treating the second top stream in a steam cracking unit to produce olefins and / or aromatics. Example 2 is the method of Example 1, wherein, in the first water treatment unit, the contacting of the hydrocarbon feed and hydrogen with the first catalyst is carried out in a first reactor unit to produce a first reactor unit effluent, and the method further includes separating the first reactor unit effluent in a first separation unit in the first water treatment unit. Embodiment 3 is the method of embodiment 1, wherein, in the second water treatment unit, the contacting of the first bottom stream with the second catalyst is carried out in the second reactor unit to produce a second reactor unit effluent, and the method further includes separating the second reactor unit effluent in a second separation unit in the second water treatment unit. Embodiment 4 is the method of embodiment 1, wherein the olefins include ethylene and / or propylene, and the aromatics include benzene. Embodiment 5 is the method of embodiment 1, wherein the first water treatment unit includes a fixed bed reactor. Embodiment 6 is the method of embodiment 1, wherein the second water treatment unit includes a boiling reactor and / or a slurry reactor. Embodiment 7 is the method of embodiment 1, wherein the hydrocarbon feed includes one or more of the following: crude oil, plastic, oligomers produced by pyrolysis of plastic, synthetic crude oil, bottom crude oil cut, bio-oil, and hydrocarbons produced by pyrolysis of plastic. Embodiment 8 is the method of embodiment 7, wherein the hydrocarbon feed includes a bottom crude oil cut stream, and the method further includes distilling the crude oil in a separation unit to produce a bottom crude oil cut stream and a top crude oil cut stream having a boiling point in the range of up to 200°C. Embodiment 9 is the method of embodiment 8, further including treating the top crude oil cut stream in a steam cracking unit to produce olefins.Embodiment 10 is the method of embodiment 1, further comprising treating the first overhead stream in a steam cracking unit to produce olefins. Embodiment 11 is the method of embodiment 1, further comprising extracting an intermediate liquid stream from the first water treatment unit, the intermediate liquid stream having a boiling point range of 200 to 305°C, and treating the intermediate liquid stream in a steam cracking unit to produce olefins. Embodiment 12 is the method of embodiment 1, wherein the first catalyst comprises one or more of the following: an organometallic compound having one or more of Ni, Mo, Co, W, Zr; NiMo; NiCoMo; NiMoW; alumina and / or zeolite. Embodiment 13 is the method of embodiment 1, wherein the second catalyst comprises a particulate hydrocracking catalyst with or without a dissolved catalyst.

[0033] Specific embodiment 14 is a system for producing olefins and / or aromatics. The system includes a first water treatment unit, the first water treatment unit has a first catalyst disposed therein, and is suitable for contacting a hydrocarbon feed and hydrogen with the first catalyst in a temperature range of 280 to 400°C, and producing a first top stream with a boiling point in the range of up to 305°C or lower and a first bottom stream including diesel and / or fuel oil and having a boiling point in the range of 305 to 650°C. The system also includes a second water treatment unit, in which a second catalyst is disposed, and the second water treatment unit is fluidly connected to the first water treatment unit, the second water treatment unit is used to contact the first bottom stream with the second catalyst in a temperature range of 400 to 500°C, and produce a second top stream, the boiling point of the top stream is in the range of 305°C or lower, and the second bottom stream includes one or more of asphalt, coke or fuel oil, and the boiling point is in the range of 305 to 650°C. The method further includes a steam cracking unit in fluid communication with the first water treatment unit and the second water treatment unit, the steam cracking unit being suitable for producing olefins and / or aromatics from the first bottom stream and the second bottom stream. Embodiment 15 is the system of embodiment 14, wherein the first water treatment unit comprises a fixed bed reactor. Embodiment 16 is the system of embodiment 14, wherein the second water treatment unit comprises a boiling reactor and / or a slurry reactor. Embodiments 17 to 20 are the systems of embodiment 14, further comprising a separation unit (flash vessel, distillation column and / or stripping unit), the separation unit being suitable for separating crude oil to produce a bottom crude oil cutting stream, the cutting stream being included in the hydrocarbon feed of the first water treatment unit. Embodiment 18 is the system of embodiment 14, wherein the separation unit is a flash vessel in fluid communication with the steam cracking unit, the system being suitable for flowing a top crude oil cutting stream having a boiling point in the range of up to 200° C. from the separation unit to the steam cracking unit. Embodiment 19 is the system of claim 17, wherein the separation unit is a distillation tower in fluid communication with the steam cracking unit, and the system is adapted to flow the top crude oil cut stream having a boiling point in the range of up to 220°C from the distillation tower to the steam cracking unit. Embodiment 20 is the system of claim 17, wherein the separation unit is a stripping unit, and the top crude oil cut stream is separated by using a stripping gas, and the stripping gas is hydrogen, saturated gas C1 to C4. The stripping unit is in fluid communication with the steam cracking unit, and the system is adapted to flow the top crude oil cut stream having a boiling point in the range of less than 220°C from the stripping unit to the steam cracking unit. Embodiment 21 is the system of embodiment 14, wherein the first water treatment unit comprises one or more distillation towers. Embodiment 22 is the system of embodiment 14, wherein the second water treatment unit comprises one or more distillation towers. Embodiment 23 is the system of embodiment 14, wherein the pyrolysis oil recovered from the steam cracker is preferentially fed to the second water treatment unit compared to the first water treatment unit. This is because the second water treatment unit is operated at a higher intensity and conversion rate than the first water treatment unit, and therefore it is necessary to reduce the accumulation of asphaltene / coke.

[0034] Unless explicitly excluded, all embodiments described above and herein can be combined in any way.

[0035] Although the embodiments of the present application and their advantages have been described in detail, it should be understood that various changes, substitutions and modifications may be made herein without departing from the spirit and scope of the embodiments defined by the appended claims. In addition, the scope of the present application is not limited to the specific embodiments of the processes, machines, manufactures, material compositions, means, methods and steps described in the specification. As those of ordinary skill in the art will readily appreciate from the above disclosure, currently existing or later developed processes, machines, manufactures, material compositions, means, methods or steps may be used, which may perform substantially the same functions or achieve substantially the same results as the corresponding embodiments described herein. Therefore, the appended claims are intended to include such processes, machines, manufactures, material compositions, means, methods or steps within their scope.

Claims

1. The method according to claim 1, wherein: within the first water treatment unit, contacting the hydrocarbon feed and hydrogen with the first catalyst is conducted in a first reactor unit to produce a first reactor unit effluent; And the method also includes: The first reactor unit effluent is separated in a first separation unit within the first water treatment unit.

2. The method according to claim 1, wherein: within the second water treatment unit, contacting the first bottoms stream with the second catalyst is performed in a second reactor unit to produce a second reactor unit effluent; And the method also includes: The second reactor unit effluent is separated in a second separation unit within the second water treatment unit.

3. The method according to claim 1, wherein: The olefins include ethylene, propylene and / or butene and butadiene, and the aromatics include benzene, toluene, xylene and ethylbenzene.

4. The method according to claim 1, wherein: The first water treatment unit includes a fixed bed reactor.

5. The method according to claim 1, wherein: The second water treatment unit includes a boiling reactor and / or a slurry reactor.

6. The method according to claim 1, wherein: The hydrocarbon feed comprises one or more of crude oil, plastics, hydrocarbons from pyrolysis of plastics, bio-oils, hydrogenated bio-oils, oligomers from plastics, synthetic crude oils and pyrolysis oils derived from plastics, bottom fractions of crude oil fractions, pyrolysis oils and residues from steam crackers.

7. The method according to claim 7, wherein: The hydrocarbon feed comprises a bottoms crude oil fraction stream, and the method further comprises: The crude oil is separated in a separation unit to produce a bottom crude oil fraction stream and a top crude oil fraction stream having a boiling point of at most 200°C.

8. The method according to claim 8, further comprising: The overhead crude fraction stream is processed in the steam cracking unit to produce olefins.

9. The method according to claim 1, further comprising: processing the first overhead stream in the steam cracking unit to produce olefins and / or further comprising: withdrawing an intermediate stream from the first water treatment unit, the intermediate stream having a boiling point of 200 to 305°C; and The intermediate stream is processed in the steam cracking unit to produce olefins.

10. The method according to claim 1, wherein: The first catalyst comprises one or more of the following: an organic metal compound having one or more of Ni, Mo, Co, W, Zr; NiMo; NiCoMo; NiMoW; alumina; and zeolite and / or The second catalyst comprises one or more of the following: an organic metal compound having one or more of Ni, Mo, Co, W, and Zr; NiMo; NiCoMo; NiMoW; alumina; and zeolite.

11. A system for producing olefins and / or aromatics, the system comprising: a first water treatment unit having a first catalyst disposed therein, adapted to contact a hydrocarbon feed and hydrogen with the first catalyst at a temperature of 280 to 400° C. and produce a first overhead stream having a boiling point of up to 200° C. or less and a first bottoms stream comprising diesel and / or fuel oil and having a boiling point of 305 to 650° C.; a second water treatment unit having a second catalyst disposed therein and in fluid communication with the first water treatment unit, the second water treatment unit being adapted to contact the first bottoms stream with the second catalyst at a temperature in the range of 400 to 500°C and produce a second overhead stream having a boiling point in the range of up to 305°C and a second bottoms stream comprising one or more of asphalt, coke or fuel oil and having a boiling point in the range of 305 to 650°C; and A steam cracking unit is in fluid communication with the first water treatment unit and the second water treatment unit, the steam cracking unit being adapted to produce olefins and / or aromatics from the first overhead stream and the second overhead stream.

12. The system according to claim 12, wherein: The first water treatment unit comprises a fixed bed reactor and / or The second water treatment unit comprises a boiling reactor and / or a slurry reactor.

13. The system of claim 12, further comprising: a separation unit adapted to separate crude oil to produce a crude oil bottoms fraction stream contained in the hydrocarbon feed to the first water treatment unit, preferably The separation unit is in fluid communication with the steam cracking unit, and the system is adapted to flow an overhead crude oil fraction stream having a boiling point in the range of up to 200°C from the separation unit to the steam cracking unit.

14. The system according to claim 14, wherein: The first water treatment unit comprises one or more distillation columns and / or wherein the second water treatment unit comprises one or more distillation columns.

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