System and process for producing hydrocarbon products using crude oil and heavy hydrocarbon feedstocks

Abstract

The invention discloses a system and a method for producing olefin products, diesel oil and fuel oil by using hydrocarbon raw materials. The system includes feeding an understream of flash crude oil to a water treatment plant, water treating the flash crude oil to produce a gas stream, diesel and fuel oil to a steam cracker, and a liquid stream to the steam cracker to produce olefins. Further treatment processes can produce ethylene, propylene and butene, as well as pitch and / or coke.

Description

[0001] CROSS-REFERENCE TO RELATED APPLICATIONS

[0002] none Background of the Invention A. Field of the Invention

[0004] The present invention generally relates to systems and methods for producing diesel and low sulfur fuel oil or lubricating oil products from hydrocarbon feedstocks, while also producing high value chemical products. A system includes a water treatment device fluidly coupled to a crude oil separation device (flasher, distillation column or stripping device), so that the heavy flashed crude oil produced from the separation device is fed to the water treatment device for treatment to produce diesel, ultra-low sulfur fuel oil and / or asphalt under certain conditions, and a liquid fraction and a gas fraction with a boiling point in the range of 35°C to 400°C. A steam cracker is also provided, and the liquid fraction from the water treatment device is fed to the steam cracker together with the gas fraction from the water treatment device and the gas fraction from the crude oil flasher, and steam cracked under conditions to produce olefins. In addition, in some configurations, the hydrocarbon feedstock is first treated in a fluid catalytic cracking device to produce high value chemicals and liquids; the liquid from the fluid catalytic cracking (FCC) device is fed to the water treatment device and then further converted into olefins in the steam cracker. The first step of FCC helps reduce coke deposition in the water treatment unit during high conversions and also helps to increase the P / E ratio. See our article on water treatment applications.

[0005] The water treatment is to hydrocracking hydrocarbons in the presence of (a) one or more water treatment catalysts and (b) a solvent that keeps asphaltene dissolved, at a temperature of 280°C to 550°C and a pressure of 40 bar to 200 barg. In an embodiment of the present invention, the water treatment conditions may include a liquid feed of 200NL / L to 2000NL / L of hydrogen to hydrocarbon ratio, and the water treatment may be carried out with or without the addition of steam. The water treatment catalyst may include a dissolving portion and a dispersing portion. The dissolving portion of the catalyst includes an organic metal compound having one or more of Ni, Mo, Co, W, and Zr. The dissolving portion of the catalyst may include metal naphthenates and / or octanoates having hydrogenation activity. The dispersing portion of the catalyst is selected from: alkali metal hydroxides or oxides, Ni-Mo oxides or sulfides, Co-Mo oxides or sulfides, W-Mo oxides or sulfides on alumina or zeolites, or any combination of these substances having hydroprocessing and / or hydrogen transfer activity.

[0006] B. Description of Related Art

[0007] Olefins (e.g., ethylene) are basic building blocks for a wide variety of commercially valuable polymers. Naturally occurring sources of olefins do not exist in commercial quantities. Therefore, polymer producers rely on methods to convert more abundant lower alkanes into olefins. The method of choice for today's commercial-scale producers is steam cracking, a highly endothermic process that briefly subjects steam-diluted alkanes to temperatures of at least 800°C. The fuel requirements to generate the required temperatures and the need for equipment that can withstand them significantly increase the overall cost. In addition, high temperatures also promote the formation of coke, which accumulates within the system, resulting in the need to shut down the reactor periodically for maintenance and coke removal, which is costly.

[0008] There are already documented descriptions of processes and systems for producing olefins from crude oil. For example, international patent application WO2017 / 133975 published by Ward et al. describes an integrated process for converting crude oil into petrochemical products, including crude oil distillation, hydrocracking, and steam cracking to produce petroleum products. Unfortunately, high conversion of ethylene in a steam cracker results in more methane gas losses, thereby reducing carbon efficiency. In addition, when attempting to convert straight-run crude oil and feed all streams directly from the hydrocracker to the steam cracker, the capacity of the steam cracker increases, not only because all streams are fed directly to the steam cracker, but also because as heavier feedstocks are converted in the steam cracker, the streams circulating to the steam cracker also increase.

[0009] In summary, while technologies exist to produce olefins, they are energy and material inefficient and costly.

[0010] Diesel is an important fuel for the automotive and trucking industries. Fuel oil is an important heating fuel for commercial and residential use and should also have a low sulfur content.

[0011] Typically, these products have been produced by subjecting various heavier crude oil fractions (such as vacuum residue) to catalytic hydrocracking processes. These hydrocracking processes are energy intensive, do not always provide adequate yields, and have high equipment costs.

[0012] Thus, while the technology exists for producing olefins, diesel and fuel oil, there is a need for new, more efficient systems and processes to make these products. The present invention allows for the extraction of diesel as a product when desired. Summary of the invention

[0013] It has been found that a solution is provided for at least one problem associated with diesel and / or fuel oil production. One aspect relates to a method for producing olefins and diesel and / or fuel oil. The method comprises feeding a hydrocarbon feedstock to a first separation unit to produce a first stream having a boiling point below 200°C and a second stream having a boiling point above 200°C; feeding the second stream to a first water treatment unit having a first catalyst and water treating a third stream at a temperature above 400°C to 500°C to produce a water treatment effluent containing 95 wt.% hydrocarbons having a boiling point below 350°C; separating the water treatment effluent to form a first stream comprising diesel having a boiling point of 220°C to 370°C; a third stream comprising fuel oil, a liquid stream having a boiling point between 35°C and 400°C, and a first gas stream having a boiling point below 200°C; feeding the first gas stream and the first stream to a steam cracker. The liquid stream is fed to a steam cracker. The first stream is fed to a steam cracker to produce olefins.

[0014] One aspect relates to a method for producing olefins and diesel and / or fuel oil, the method comprising the following steps: feeding a hydrocarbon feedstock to a first separation unit to produce a first stream having a boiling point below 200°C and a second stream having a boiling point above 200°C; feeding the second stream to a first water treatment unit having a first catalyst, and water treating a third stream at a temperature above 400°C to 500°C to produce a water treatment effluent containing 95 wt% of hydrocarbons and having a boiling point below 350°C; separating the water treatment effluent to form a first stream comprising diesel having a boiling point of 220°C to 370°C; a third stream comprising fuel oil, a liquid stream having a boiling point between 35°C and 400°C, and a second gas stream having a boiling point below 200°C; combining the second gas stream and the first stream to form a mixed gas stream; feeding the mixed gas stream into steam; and steam cracking the liquid stream in a steam cracker to produce olefins.

[0015] One aspect relates to a method for producing olefins and diesel and / or fuel oil, the method comprising the following steps: feeding a hydrocarbon feedstock to a first separation device to produce a first stream having a boiling point below 200° C. and a second stream having a boiling point above 200° C.; feeding the second stream to a first water treatment device having a first catalyst, and water treating a third stream at a temperature above 400° C. to 500° C. to produce a water treatment effluent containing 95 wt.% of hydrocarbons having a boiling point below 350° C.; separating the water treatment effluent to form a first stream having a boiling point of 220° C.; ℃ to 370℃ diesel; a third stream comprising fuel oil, a liquid stream with a boiling point of 35℃ to 400℃ and a third gas stream with a boiling point below 200℃; combining the third gas stream and the first stream to form a mixed gas stream; feeding the mixed gas stream to a second flash device to produce a flash product; separating the flash product into a stream comprising ethane, a stream comprising butane and a stream comprising propane; feeding the stream comprising ethane to a steam cracker; and steam cracking the stream comprising ethane in the steam cracker to produce olefins.

[0016] One aspect relates to a method for processing hydrocarbons, the method comprising the steps of: feeding a hydrocarbon feedstock to an optional first separation device to produce a first stream having a boiling point below 200°C and a second stream having a boiling point above 200°C; feeding the first stream to a first steam cracker; feeding the second stream or the hydrocarbon feedstock to a first fluid catalytic cracker having a first catalyst, and in the first fluid catalytic cracker, cracking the second stream by contacting the second stream with the first catalyst at a temperature of 450°C to 730°C to produce a second stream having a boiling point of 35°C to 550°C; A method of producing olefins comprising: producing a first liquid stream and a gaseous effluent comprising C1 to C4 hydrocarbons; feeding the first liquid stream to a first water treatment device having a first catalyst, the first catalyst comprising a particulate catalyst and a dissolved catalyst; and water treating the first liquid stream at a temperature of 330°C to 500°C to produce a water treatment effluent having a boiling point not exceeding 400°C; separating the water treatment effluent to form a second liquid stream having a boiling point of 200°C to 400°C and a gas stream having a boiling point below 200°C; feeding the gas stream and the second liquid stream to a first steam cracker; and steam cracking in the steam cracker to produce olefins.

[0017] Other embodiments of the present invention are also discussed in this application. Any embodiment discussed about one aspect of the present invention is also applicable to other aspects of the present invention, and vice versa. Each embodiment described herein is understood to be an embodiment of the present invention applicable to other aspects of the present invention. It can be considered that any embodiment or aspect discussed herein can be combined with other embodiments or aspects discussed herein and / or implemented with respect to any method or composition of the present invention, and vice versa. In addition, composition of the present invention can be used to realize method of the present invention.

[0018] Included below are definitions of various terms and phrases used throughout this specification.

[0019] The term "C# hydrocarbons", where "#" is a positive integer, refers to hydrocarbons having # carbon atoms. Additionally, the term "C#+ hydrocarbons" refers to hydrocarbon molecules having # or more carbon atoms. Thus, the term "C2+ hydrocarbons" refers to a mixture of hydrocarbons having 2 or more carbon atoms. The term "C2+ alkanes" refers to alkanes having 2 or more carbon atoms.

[0020] "Cracking" refers to a process involving the decomposition of organic compounds and the reorganization of molecules to produce a greater number of molecules than originally present. During the cracking process, a series of reactions occur with the transfer of hydrogen atoms between molecules. For example, naphtha can undergo thermal cracking reactions to produce ethylene and hydrogen.

[0021] "Hydrocarbons" are generally defined as molecules formed primarily of carbon and hydrogen atoms. Hydrocarbons may also include other elements, such as, but not limited to, halogens, metallic elements, nitrogen, oxygen, and / or sulfur. Hydrocarbon fluids may include, be entrained with, or be entrained in non-hydrocarbon fluids (e.g., hydrogen, nitrogen, carbon monoxide, carbon dioxide, hydrogen sulfide, water, and / or ammonia).

[0022] The term "about" or "approximately" is defined as close to what one of ordinary skill in the art understands. In a non-limiting embodiment, the term is defined as within 10%, preferably within 5%, more preferably within 1%, and most preferably within 0.5%.

[0023] The terms "wt. %, "vol. %" or "mol. %" refer to the weight percentage, volume percentage or mole percentage of a component based on the total weight, total volume or total moles of the material including the component, respectively. In a non-limiting example, 10 grams of a component in 100 grams of material is 10 wt. %.

[0024] The term "substantially" and variations thereof are defined to include ranges within 10%, within 5%, within 1% or within 0.5%.

[0025] When used in the claims and / or specification, the terms "inhibit" or "reduce" or "prevent" or "avoid" or any variation of these terms includes any measurable reduction or complete inhibition to achieve the desired result.

[0026] The term "effective" as used in the specification and / or claims means sufficient to achieve a desired, intended, or intended result.

[0027] The use of the words "a" or "an" when used in conjunction with any of the terms "comprising," "including," "containing," or "having" in the claims or description may mean "one," but is also consistent with the meanings of "one or more," "at least one," and "one or more."

[0028] The words "comprise" (and any forms of comprising, such as "include" and "contain"), "have" (and any forms of having, such as "have" and "have"), "include" (and any forms of including, such as "include" and "containing"), or "contains" (and any forms of containing, such as "including" and "containing") are inclusive or open-ended and do not exclude additional, unrecited elements or method steps.

[0029] The systems and processes of the present invention may "comprise," "consist essentially of," or "consist of" specific ingredients, components, compositions, etc. disclosed throughout the specification. With respect to the transition phrase "consisting essentially of," in one non-limiting aspect, the fundamental and novel characteristic of the systems and methods of the present invention is that they are capable of producing olefin products (e.g., ethylene) in a cost and energy efficient manner by having a steam cracker capable of receiving ethane from a mixed feed steam cracker and feeding C2+ products produced by the ethane steam cracker to the mixed feed steam cracker.

[0030] Other objects, features and advantages of the present invention will become apparent through the following drawings, detailed descriptions and examples. However, it should be understood that although the drawings, detailed descriptions and examples indicate specific embodiments of the present invention, they are only given by way of illustration and are not intended to be restrictive. In addition, changes and modifications within the spirit and scope of the present invention will 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 an embodiment may be combined with the features of any other embodiment. In more embodiments, other additional features may also be added to the specific embodiments described herein. BRIEF DESCRIPTION OF THE DRAWINGS

[0031] Advantages of the present invention may become apparent to those skilled in the art from the following detailed description with reference to the accompanying drawings.

[0032] Figure 1 One embodiment of a system for producing olefins, diesel and / or fuel oil products from a hydrocarbon feedstock provided to a water treatment unit is shown.

[0033] Figure 2 One embodiment of a system for producing diesel, fuel oil, and olefin products from a hydrocarbon feedstock provided to a water treatment unit is shown.

[0034] Figure 3 A configuration with an upstream fluid catalytic cracking (FCC) unit is shown.

[0035] While the invention is susceptible to various modifications and alternative forms, specific embodiments thereof are shown by way of example in the drawings. The drawings may not be drawn to scale.

[0036] Detailed description of the invention

[0037] It has been found that a solution to at least one problem associated with preparing olefins and diesel and / or fuel oil is provided. In one aspect, a mixed hydrocarbon feedstock can be fed to a mixed hydrocarbon steam cracker to produce petroleum products and ethane. Ethane can be provided to an independent ethane cracking unit to produce ethylene and / or C2+ hydrocarbon streams, which can be recycled to the mixed hydrocarbon steam cracker. The advantage of this device is that the mixed hydrocarbon steam cracker can carry out C2+ cracking under optimal conditions, and the ethane steam cracker can crack ethane under optimal conditions. These and other non-limiting aspects of the present invention are discussed in further detail below with reference to the accompanying drawings.

[0038] Reference Figure 1 , describes a system 100 for producing olefin products. System 100 may include a crude oil flash unit 102, a steam cracker 104, and a water treatment unit 106. Crude oil 101 enters the crude oil flash unit 102, where it is flashed to produce a stream 103 with a cut point below 200°C and a bottom stream 105 that is fed to the water treatment unit 106. Stream 103 can be fed to the steam cracker 104. Hydrogen 112 is also fed to the water treatment unit 106. The bottom stream 105 is water treated in the water treatment unit, and the resulting liquid stream 109 is fed to the steam cracker 104. A gas stream 110 from the water treatment unit 106 is also fed to the steam cracker 106. All feeds in the steam cracker 104 can be treated under conditions that produce olefins 111. The water treatment unit will also produce diesel 107 and a fuel oil stream 108 containing fuel oil.

[0039] Crude oil 101 can be the oil of unrefined form extracted from geological formation.Term crude oil can also include oil after water-oil separation and / or gas-oil separation and / or desalting and / or stabilization treatment.Non-limiting examples of crude oil include Arabian heavy crude oil, Arabian light crude oil, other Gulf crude oil, Brent crude oil, North Sea crude oil, North Africa and West Africa crude oil, Indonesian crude oil, Chinese crude oil, West Texas crude oil and mixtures thereof, also include shale oil, asphalt sand, natural gas condensate and bio-based oil.The crude oil used as feed of the process of the present invention is preferably conventional oil with an API gravity greater than 20 ° API measured by ASTM D287 standard.On the one hand, the crude oil used in the process of the present invention is a light crude oil with an API gravity greater than 30 ° API.On the other hand, the crude oil used in the process of the present invention can include Arabian light crude oil.The API gravity of Arabian light crude oil is usually between 32 °-36 ° API, and the sulfur content is between 1.5wt.%-4.5wt.%.

[0040] Reference Figure 2, shows an alternative process in which a gas stream 110 from a water treatment unit 106 is combined with stream 103 and the combined stream is sent to a steam cracker unit 104.

[0041] Alternatively, the mixed gas stream 115 may be fed to a distillation unit 116, ethane 118 separated and fed to a steam cracker 115. A propane stream 117 may also be separated in the distillation unit 116 and fed to a propane dehydrogenation unit 120 or a propane steam cracker to produce propylene 121. Similarly, a butane stream may be separated from the distillation unit 116 and fed to a butane dehydrogenation unit or a butane steam cracker 122 to produce C4 olefins 123 or to a butane to ethane conversion unit, whereby ethane is fed to an ethane steam cracker to produce ethylene. The propylene stream 121 and the C4 olefin stream 123 may be combined into a stream 124 and recovered.

[0042] Now refer to Figure 3 , a hydrocarbon feedstock 201 (which may be crude oil) is fed to a separation device 202, where it is separated into a stream 203 having a boiling point below 200°C and a stream 204 having a boiling point above 200°C.

[0043] The stream 203 having a boiling point below 200° C. is fed to a steam cracker 209 and is steam cracked to produce a steam cracking effluent 216 , which is separated into a final product 214 comprising olefins.

[0044] The stream 204 having a boiling point above 200°C is fed to a fluid catalytic cracking (FCC) unit 215 containing an FCC processing catalyst, preferably a catalyst containing a zeolite, more preferably a ZSM-5, HY zeolite, NaY zeolite, SAPO011 zeolite, MCM-41 zeolite, and treated under certain conditions to produce a bottom stream 207 and an overhead stream 206, which is fed to a downstream separation unit 210. The conditions may include 400°C to 900°C, more preferably 500°C to 800°C, more preferably 600°C to 700°C, and any range therein, including the endpoint temperatures.

[0045] The bottom stream 207 is fed to a water treatment unit 211 and treated under conditions to produce diesel 212, fuel oil 213 and a water treated top stream 208 which is fed to a steam cracker downstream separation unit 210.

[0046] In certain aspects, the other hydrocarbon feedstock 114 may be combined with the crude oil 101 prior to entering the crude oil flash unit, or may be combined with the bottom feed 105 prior to entering the water treatment unit 106 , and optionally with the hydrogen 112 .

[0047] Unit 122 may also be a butane dehydrogenation unit or a butane to ethane conversion unit from which the ethane is fed to an ethane cracker.

[0048] In the steam cracking process, saturated hydrocarbons are broken down into smaller, usually unsaturated hydrocarbons, such as ethylene and propylene, by diluting a mixed hydrocarbon feed with steam and heating the mixture in a furnace in the absence of oxygen. The residence time of the steam cracking reaction is 50 milliseconds to 1000 milliseconds. The hybrid steam cracker may have a fractionation unit (not shown) or a gas fractionation unit (not shown) capable of separating ethane from the olefin product stream. Such fractionation units are well known in the art.

[0049] The ethane stream 118 may include other gaseous compounds such as propane and butane. In the steam cracker 104, the gaseous ethane may be diluted with steam and heated to a temperature of 775°C to 860°C (e.g., 775°C, 800°C, 825°C, 850°C, 860°C, or any value or range therebetween) and / or a pressure of 0.2 MPa to 0.3 MPa (e.g., 0.2 MPa, 0.21 MPa, 0.22 MPa, 0.23 MPa, 0.24 MPa, 0.25 MPa, 0.26 MPa, 0.27 MPa, 0.28 MPa, 0.30 MPa, or any value or range therebetween), in one or more furnaces, to produce ethylene and / or C2+ hydrocarbons and higher olefins, i.e., C3+.

[0050] Various aspects relate to a method for producing olefins and diesel and / or fuel oil, the method comprising the steps of: feeding a hydrocarbon feedstock into a first separation unit to produce a first stream having a boiling point below 200°C and a second stream having a boiling point above 200°C; feeding the second stream into a first water treatment unit having a first catalyst and water treating the second stream at a temperature above 400°C to 500°C to produce a water treatment effluent containing 95 wt.% hydrocarbons having a boiling point below 350°C; separating the water treatment effluent to form a first stream containing diesel having a boiling point of 220°C to 370°C; a third stream containing fuel oil, a liquid stream having a boiling point of 35°C to 400°C, and a first gas stream having a boiling point below 200°C; feeding the first gas stream and the first stream to a steam cracker; and steam cracking the first gas stream and the first stream in the steam cracker to produce olefins. It should be noted that the amount of diesel and fuel oil depends on the severity of the water treatment. For example, when the temperature of the water treatment reactor is 450°C, the proportion of fuel oil is 1%-2%. The liquid stream can also be fed to a steam cracker. A second liquid stream is generated in the first flash device and the second liquid stream is fed to the steam cracker, wherein the boiling point of the second liquid stream is 35°C to 200°C. The hydrocarbon feedstock comprises crude oil. The water treatment device comprises a fixed bed reactor. The water treatment catalyst comprises a particle catalyst and a dissolved catalyst.

[0051] Aspects relate to a method for producing olefins and diesel, the method comprising the steps of: feeding a hydrocarbon feedstock into a first separation unit to produce a first stream having a boiling point below 200°C and a second stream having a boiling point above 200°C; feeding the second stream into a first water treatment unit having a first catalyst, and water treating a third stream at a temperature above 400°C to 500°C to produce a water treatment effluent with 95% boiling point below 350°C; separating the water treatment effluent to form a first stream comprising diesel having a boiling point of 220 to 370°C; a third stream comprising fuel oil, a liquid stream having a boiling point of 35°C to 400°C, and a second gas stream having a boiling point below 200°C; combining the second gas stream and the first stream to form a mixed gas stream; feeding the liquid stream to a steam cracker. Feeding the mixed gas stream to a steam cracker; and steam cracking the mixed gas stream in the steam cracker to produce olefins. In some aspects, a second liquid stream is produced in a flash unit and fed to a steam cracker, wherein the second liquid stream has a boiling point of 35°C to 200°C. The hydrocarbon feedstock comprises crude oil. In some aspects, the water treatment unit comprises a fixed bed reactor. The water treatment catalyst comprises a particulate catalyst and a dissolved catalyst.

[0052] Aspects relate to a method for producing olefins and diesel, the method comprising the steps of: feeding a hydrocarbon feedstock into a first separation device to produce a first stream having a boiling point below 200°C and a second stream having a boiling point above 200°C; feeding the second stream into a first water treatment device having a first catalyst, and water treating a third stream at a temperature above 400°C to 500°C to produce a water treatment effluent having a boiling point of 95% below 350°C; separating the water treatment effluent to form a first stream having a boiling point of 220°C to 370°C; A first stream of diesel; a third stream comprising fuel oil, a liquid stream having a boiling point of 35°C to 400°C, and a third gas stream having a boiling point below 200°C; combining the third gas stream and the first stream to form a mixed gas stream; feeding the mixed gas stream to a second distillation unit to produce a distillation product; separating the distillation product into a stream comprising ethane, a stream comprising butane, and a stream comprising propane; feeding the stream comprising ethane to a steam cracker; steam cracking the stream comprising ethane in a steam cracker to produce olefins. The stream comprising propane enters a propane dehydrogenation unit or a propane steam cracker. Various aspects include feeding a stream comprising butane to a butane dehydrogenation unit or a butane steam cracker to produce olefins or feeding butane to a butane to ethane conversion unit, and then feeding the produced ethane to an ethane steam cracker to produce olefins.

[0053] The hydrocarbons may comprise one or more of the following: crude oil, plastics, oligomers from pyrolysis of plastics, synthetic crude oil, hydrocarbons from crude oil fractions and pyrolysis of plastics, bio-oils.

[0054] When the steam cracker is in operation, the mass ratio of propylene to ethylene (P / E) is 0.45-0.68, preferably 0.6-0.68.

[0055] Various aspects relate to a method for processing hydrocarbons, the method comprising the steps of: feeding a hydrocarbon feedstock to an optional first separation device to produce a first stream having a boiling point below 200° C. and a second stream having a boiling point above 200° C.; feeding the first stream to a first steam cracker; feeding the second stream or the hydrocarbon feedstock to a first fluid catalytic cracker having a first catalyst, and cracking the second stream in the first fluid catalytic cracker by contacting the second stream with the first catalyst at a temperature of 450° C. to 730° C. to produce a first stream having a boiling point of 35° C. to 55° C.; The invention relates to a method for preparing a first liquid effluent having a temperature of 0°C and a gaseous effluent comprising C1 to C4 hydrocarbons; feeding the first liquid stream to a first water treatment device having a first catalyst, and water treating the first liquid stream at a temperature of 330°C to 500°C to produce a water treatment effluent having a boiling point not exceeding 400°C; separating the water treatment effluent to form a second liquid stream having a boiling point of 200°C to 400°C, and a gas stream having a boiling point below 200°C; feeding the gas stream and the second liquid stream to a first steam cracker; steam cracking the gas stream and the second liquid stream in the steam cracker to produce olefins. The overall P / E ratio of the hydrocarbon feedstock is preferably greater than 0.55.

[0056] Non-limiting examples of the present invention are now described. Example 1 is a method for producing olefins and diesel and / or fuel oil. The method includes the following steps: feeding a hydrocarbon feedstock into a first separation device to produce a first stream having a boiling point below 200°C and a second stream having a boiling point above 200°C; feeding the second stream into a first water treatment device having a water treatment catalyst, and water treating the second stream at a temperature above 400°C to 500°C to produce a water treatment effluent, the effluent containing 95% by weight of hydrocarbons and 95% having a boiling point below 350°C, separating the water treatment effluent to form a third stream containing diesel having a boiling point of 220°C to 370°C; a fourth stream containing fuel oil, a liquid stream having a boiling point of 35°C to 400°C and a first gas stream having a boiling point below 200°C; feeding the first gas stream and the first stream to a steam cracker; fully producing olefins under the conditions of steam cracking the first gas stream and the first stream in the steam cracker. Embodiment 2 is the method of embodiment 1, further comprising the step of supplying the liquid stream to the steam cracker. Embodiment 3 is the method of claim 1, generating a second liquid stream in the first flash unit, and feeding the second liquid stream to the steam cracker, the second liquid stream having a boiling point of 35°C to 200°C. Embodiment 4 is the method of embodiment 1, the hydrocarbon feedstock comprises crude oil. Embodiment 5 is the method of embodiment 1, the first water treatment unit comprises a fixed bed reactor. Embodiment 6 is the method of claim 1, the water treatment catalyst comprises a dispersed catalyst and a dissolved catalyst. Embodiment 7 is the method of claim 6, the dissolved catalyst comprises an organometallic compound having one or more of Ni, Mo, Co, W, Zr, preferably in the form of a metal naphthenate and / or octanoate, and / or the dispersed catalyst is selected from: alkali metal hydroxides or oxides, Ni-Mo oxides, Ni-Mo sulfides, Co-Mo oxides or Co-Mo sulfides, W-Mo oxides, W-Mo sulfides, preferably on alumina or zeolites, or any combination of these substances.

[0057] Example 8 is a method for producing olefins and diesel. The method includes the following steps: feeding a hydrocarbon feedstock into a first separation device to produce a first stream with a boiling point below 200°C and a second stream with a boiling point above 200°C; feeding the second stream into a first water treatment device having a first catalyst, and water treating the second stream at a temperature above 400°C to 500°C to produce a water treatment effluent containing 95% and a boiling point below 350°C; separating the water treatment effluent to form a first stream containing diesel with a boiling point of 220°C to 370°C; a third stream containing fuel oil, a liquid stream with a boiling point of 35°C to 400°C, and a second gas stream with a boiling point below 200°C; combining the second gas stream and the first stream to form a mixed gas stream; feeding the mixed gas stream to a steam cracker; steam cracking the mixed gas stream in the steam cracker to produce olefins. Example 9 is the method of Example 8, further comprising the step of feeding the liquid stream and the fuel oil to the steam cracker. Embodiment 10 is the method of embodiment 8, wherein a second liquid stream is produced in a flash unit and the second liquid stream is fed to a steam cracker, wherein the second liquid stream has a boiling point of 35°C to 200°C. Embodiment 11 is the method of embodiment 8, wherein the hydrocarbon feedstock comprises crude oil. Embodiment 12 is the method of embodiment 8, wherein the first water treatment unit comprises a fixed bed reactor. Embodiment 13 is the method of embodiment 8, wherein the first catalyst comprises a particulate catalyst and a dissolved catalyst. Embodiment 14 is the method of embodiment 11, wherein the dissolved catalyst comprises an organometallic compound having one or more of Ni, Mo, Co, W, Zr, preferably in the form of a metal naphthenate and / or octanoate, and / or a dispersed catalyst selected from the group consisting of an alkali metal hydroxide or oxide, Ni-Mo oxide, Ni-Mo sulfide, Co-Mo oxide or Co-Mo sulfide, W-Mo oxide, W-Mo sulfide, preferably on alumina or zeolite, or any combination of these substances.

[0058] Embodiment 15 is a method for producing olefins and diesel, the method comprising the following steps: feeding a hydrocarbon feedstock into a first separation device to produce a first stream having a boiling point below 200°C and a second stream having a boiling point above 200°C; feeding the second stream into a first water treatment device having a first catalyst, and water treating the second stream at a temperature above 400°C to 500°C to produce a water treatment effluent containing 95% of hydrocarbons and having a boiling point below 350°C; separating the water treatment effluent to form a first stream containing hydrocarbons having a boiling point of 220°C to 3 A first stream of 70°C diesel; a third stream containing fuel oil, a liquid stream with a boiling point of 35°C-400°C, and a third gas stream with a boiling point below 200°C; combining the third gas stream and the first stream to form a mixed gas stream; feeding the mixed gas stream to a second flash unit to produce a flash product; separating the flash product into an ethane-containing stream, a butane-containing stream and a propane-containing stream; feeding the ethane-containing stream to a steam cracker; steam cracking the ethane-containing stream in a steam cracker to produce olefins. Example 16 is the method of Example 15, further comprising the step of feeding the propane-containing stream to a propane dehydrogenation unit or a propane steam cracker. Example 17 is the method of claim 15, further comprising the step of feeding the butane-containing stream to a butane dehydrogenation unit or a butane steam cracker.

[0059] Embodiment 18 is the method of any of the above embodiments, wherein the hydrocarbon feedstock comprises one or more of: crude oil, plastic, oligomers from plastic pyrolysis, synthetic crude oil, crude oil fractions, hydrocarbons from plastic pyrolysis, and bio-oil. Embodiment 19 is the method of any of the above embodiments, wherein the steam cracker is operated in a mass ratio of propylene to ethylene (P / E) of 0.6 to 0.68.

[0060] Embodiment 20 is a method for processing hydrocarbons, which comprises the following steps: feeding a hydrocarbon feedstock into an optional first flash device to produce a first stream having a boiling point below 200°C and a second stream having a boiling point above 200°C; feeding the first stream into a first steam cracker; feeding the second stream or the hydrocarbon feedstock into a first fluid catalytic cracker having a first catalyst, and cracking the second stream or the hydrocarbon feedstock in the first fluid catalytic cracker by contacting the second stream with the first catalyst at a temperature of 450°C to 730°C to produce a first liquid effluent having a boiling point of 35°C to 550°C and a gaseous effluent containing C1 to C4 hydrocarbons; feeding the first liquid stream into a first water treatment device of the first catalyst, wherein the catalyst contains a particulate catalyst and a dissolved catalyst. The first liquid stream is subjected to water treatment at a temperature of 330°C to 500°C to produce a water treatment effluent with a boiling point not exceeding 400°C; the water treatment effluent is separated to form a second liquid stream with a boiling point of 200°C to 400°C and a gas stream with a boiling point below 200°C; the gas stream and the second liquid stream are fed to a first steam cracker; and the gas stream and the second liquid stream are steam cracked in the steam cracker to produce olefins, preferably, the P / E of the product is greater than 0.55 overall.

[0061] Embodiment 21 is the method of any of embodiments 1-20, wherein the P / E ratio of the product is 0.55. Embodiment 22 is the method of embodiment 20, wherein the steam cracker is operated at a P / E mass ratio of 0.45 to 0.68. Embodiment 23 is the method of any of the above claims, wherein the water treatment unit is a fixed bed unit.

[0062] *****

[0063] Although the embodiments and advantages thereof of the present application 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 intended to be limited to the specific embodiments of the processes, machines, manufactures, material compositions, means, methods and steps described in the specification. As will be readily understood by those of ordinary skill in the art from the above content, processes, machines, manufactures, material compositions, means, methods or steps that currently exist or will be developed to perform substantially the same functions or achieve substantially the same results may be used to replace 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. A method for producing olefins and diesel and / or fuel oil, characterized in that: The method comprises the following steps: Feeding a hydrocarbon feedstock to a first separation device to produce a first stream having a boiling point below 200° C. and a second stream having a boiling point above 200° C.; feeding the second stream to a first water treatment unit having a water treatment catalyst and water treating the second stream at a temperature greater than 400°C to 500°C to produce a water treatment effluent containing 95% by weight hydrocarbons having a 95% boiling point less than 350°C; Separating the water treatment effluent to form a third stream comprising diesel with a boiling point of 220°C to 370°C; a fourth stream comprising fuel oil, a liquid stream with a boiling point of 35°C to 400°C and a first gas stream with a boiling point below 200°C; feeding the first gas stream and the first feed stream to a steam cracker; and The first gas stream and the first feed stream are steam cracked in a steam cracker under sufficient conditions to produce olefins.

2. The method according to claim 1, characterized in that The following steps are also included: The liquid stream is fed to a steam cracker.

3. The method according to claim 1, characterized in that A second liquid stream is produced in the first flash unit and fed to a steam cracker, the second liquid stream having a boiling point of 35°C to 200°C.

4. The method according to claim 1, characterized in that The hydrocarbon feedstock comprises crude oil.

5. The method according to claim 1, characterized in that The first water treatment device includes a fixed bed reactor.

6. The method according to claim 1, characterized in that Water treatment catalysts include dispersed catalysts and dissolved catalysts. Preferably, The dissolved catalyst comprises one or more organometallic compounds having Ni, Mo, Co, W, Zr, preferably in the form of metal naphthenates and / or octoates, and / or the dispersed catalyst is selected from: alkali metal hydroxides or oxides, Ni-Mo oxides, Ni-Mo sulfides, Co-Mo oxides or Co-Mo sulfides, W-Mo oxides, W-Mo sulfides, preferably on alumina or zeolites, or any combination of these substances.

7. A method for producing olefins and diesel, characterized in that: The method comprises the following steps: Feeding a hydrocarbon feedstock into a first separation device to produce a first stream having a boiling point below 200° C. and a second stream having a boiling point above 200° C.; feeding the second stream to a first water treatment unit having a first catalyst and hydrotreating the second stream at a temperature greater than 400°C to 500°C to produce a water treatment effluent having 95% boiling point less than 350°C; Separating the water treatment effluent to form a first stream comprising diesel having a boiling point of 220°C to 370°C, a third stream comprising fuel oil, a liquid stream having a boiling point of 35°C to 400°C and a second gas stream having a boiling point below 200°C; combining the second gas stream and the first stream to form a mixed gas stream; feeding the mixed gas stream to a steam cracker; and The mixed gas stream is steam cracked in a steam cracker to produce olefins.

8. The method according to claim 7, characterized in that Also comprising the step of feeding the liquid stream and fuel oil to a steam cracker, and / or A second liquid stream is produced in the flash unit and fed to the steam cracker, the second liquid stream having a boiling point of 35°C to 200°C.

9. The method according to claim 7, characterized in that: The hydrocarbon feedstock comprises crude oil, and / or The first water treatment device includes a fixed bed reactor.

10. The method according to claim 7, characterized in that The first catalyst preferably includes a particulate catalyst and a dissolved catalyst; The dissolved catalyst comprises one or more organometallic compounds with Ni, Mo, Co, W, Zr, preferably in the form of metal naphthenates and / or octoates, and / or a dispersed catalyst selected from: alkali metal hydroxides or oxides, Ni-Mo oxides, Ni-Mo sulfides, Co-Mo oxides or Co-Mo sulfides, W-Mo oxides, W-Mo sulfides, preferably on alumina or zeolites, or any combination of these substances.

11. A method for producing olefins and diesel, characterized in that: The method comprises the following steps: Feeding a hydrocarbon feedstock to a first separation device to produce a first stream having a boiling point below 200° C. and a second stream having a boiling point above 200° C.; feeding the second stream to a first water treatment unit having a first catalyst and hydrotreating the second stream at a temperature greater than 400°C to 500°C to produce a water treatment effluent having 95% boiling point less than 350°C; Separating the water treatment effluent to form a first stream comprising diesel having a boiling point of 220°C to 370°C; a third stream comprising fuel oil, a liquid stream having a boiling point of 35°C to 400°C and a third gas stream having a boiling point below 200°C; combining the third gas stream and the first stream to form a mixed gas stream; feeding the mixed gas stream to a second flash device to produce a flash product; separating the flash product into a stream comprising ethane, a stream comprising butane, and a stream comprising propane; feeding the ethane-containing stream to a steam cracker; and A stream comprising ethane is steam cracked in a steam cracker to produce olefins.

12. The method according to claim 11, characterized in that Also includes feeding a stream comprising propane to a propane dehydrogenation unit or a propane steam cracker, and / or Further comprising feeding the butane-containing stream to a butane dehydrogenation unit or a butane steam cracker.

13. The method according to any one of the preceding claims, characterized in that The hydrocarbon feedstock comprises one or more of the following: crude oil, plastics, oligomers produced by pyrolysis of plastics, synthetic crude oil, crude oil fractions, hydrocarbons produced by pyrolysis of plastics, and bio-oil.

14. The method according to any one of the preceding claims, characterized in that The steam cracker is operated so that the mass ratio of propylene to ethylene (P / E) is between 0.6 and 0.

68.

15. A method for treating hydrocarbons, characterized in that: The method comprises the following steps: Feeding a hydrocarbon feedstock to an optional first flash unit to produce a first stream having a boiling point below 200° C. and a second stream having a boiling point above 200° C.; feeding the first stream to a first steam cracker; feeding the second stream or hydrocarbon feedstock to a first fluid catalytic cracker having a first catalyst, and cracking the second stream or hydrocarbon feedstock in the first fluid catalytic cracker by contacting the second stream with the first catalyst at a temperature of 450° C. to 730° C. to produce a first liquid effluent having a boiling point of 35° C. to 550° C. and a gaseous effluent comprising C1 to C4 hydrocarbons; feeding a first liquid stream to a first water treatment unit having a first catalyst, the first catalyst comprising a particulate catalyst and a dissolved catalyst, and hydrotreating the first liquid stream at a temperature of 330°C to 500°C to produce a water treatment effluent having a boiling point of no more than 400°C; separating the water treatment effluent to form a second liquid stream having a boiling point of 200°C to 400°C and a gas stream having a boiling point below 200°C; feeding the gas stream and the second liquid stream to the first steam cracker; and The gas stream and the second liquid stream are steam cracked in a steam cracker to produce a total olefin product having a P / E greater than 0.

55.

16. The method according to any one of claims 1 to 15, characterized in that The P / E ratio of the product was 0.

55.

17. The method according to claim 16, characterized in that The steam cracker is operated at a P / E mass ratio between 0.45 and 0.

68.

18. A method according to any one of the preceding claims, characterised in that The water treatment plant is a fixed bed plant.

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