CN113025378A - Crude oil processing method and system for increasing olefin yield - Google Patents
Crude oil processing method and system for increasing olefin yield Download PDFInfo
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- CN113025378A CN113025378A CN202110220225.8A CN202110220225A CN113025378A CN 113025378 A CN113025378 A CN 113025378A CN 202110220225 A CN202110220225 A CN 202110220225A CN 113025378 A CN113025378 A CN 113025378A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
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Abstract
The present disclosure relates to a crude oil processing method and system for increasing olefin production. According to the method, crude oil and steam are introduced into a flash separator for first separation, so that a light-phase component and a heavy-phase component can be obtained, and the separated light-phase component and the separated heavy-phase component are respectively cracked; the light component is subjected to second separation by adopting a group composition separation device, so that an aromatic hydrocarbon component and a non-aromatic hydrocarbon component can be obtained, wherein the non-aromatic hydrocarbon component can be used for preparing components such as ethylene, propylene and the like by steam cracking; the heavy phase component is catalytically cracked, so that the yield of ethylene and propylene is improved; further, the steam cracking heavy oil and the catalytic cracking slurry oil are converted into catalytic cracking raw materials through a residual oil hydrocracking device; the method realizes the integrated treatment of the light and heavy phase components of the crude oil, improves the resource utilization efficiency, and is beneficial to realizing the flexible optimization of low-carbon olefins, oil products and aromatic hydrocarbon products.
Description
Technical Field
The disclosure relates to the field of petrochemical industry, in particular to a crude oil processing method and system for producing olefin more.
Background
The dependence degree of crude oil on the outside in China is increased year by year, and the energy safety faces serious challenges. According to statistics, in 2019, the external prestorage degree of crude oil in China exceeds 70%, how to efficiently utilize crude oil resources to meet the requirements of national development and people's life is a key problem of constant exploration and research in the petrochemical industry in China.
Meanwhile, the oil refining capacity of China is continuously improved, and the market of oil products is intensified and surplus. The refinery taking the fuel oil type as the main part is accelerating to be transformed and upgraded into the refinery integration, and oil refining and chemical engineering in China enter the deep fusion and high-quality development stage. At present, newly-built enterprises adopt an integrated refining development mode, and more chemical refineries are provided with oil as an auxiliary material.
In the process of the transformation of refineries into chemical engineering, a large number of oil refining technologies and chemical technologies are rapidly developed and applied to industries, such as residual oil hydrocracking technology, heavy oil catalytic cracking technology, distillate oil conversion technology, aromatic hydrocarbon production technology, light hydrocarbon comprehensive utilization technology, crude oil steam cracking technology and the like. The technologies fully utilize the composition property difference of crude oil, residual oil, heavy oil, distillate oil, light hydrocarbon and the like, realize the purposes of increasing the production of chemical raw materials and reducing oil products from the aspect of processing different resources, and become a key supporting technology for transformation of refineries.
For a refinery, a single technical advantage has a very limited impact on the overall plant benefit. The limitation can be broken through only by integrating a plurality of single-point key technologies from the global perspective, so that the resources (crude oil resources, equipment resources, land resources, human resources and the like) are more efficiently and reasonably utilized, the structural quality of the product is more optimized and the quality is more improved, and the petrochemical industry is better assisted to develop to higher quality.
Disclosure of Invention
The purpose of this disclosure is to provide a crude oil processing method and system for the production of olefins. The method can integrate the light phase treatment and the heavy phase treatment of the crude oil, synchronously solve the efficient processing problem of the light component and the heavy component of the crude oil, greatly improve the yield of low-carbon olefin products, reduce the yield of oil products, and realize the flexible optimization of the olefin products, the oil products and the aromatic hydrocarbon products.
In order to achieve the above object, the present disclosure provides a method for processing crude oil with high yield of olefins, comprising the steps of:
s1, enabling the crude oil and the steam to enter a flash separator for first separation, and separating out a light phase component and a heavy phase component;
s2, enabling the light phase component to enter a group composition separation device for secondary separation, and separating a non-aromatic component and an aromatic component;
s3, feeding the non-aromatic hydrocarbon components into a radiation area of a steam cracking device for steam cracking to obtain ethylene, propylene, steam cracking heavy oil and a first C4-C5 component;
s4, enabling the heavy phase component to enter a catalytic cracking integrated device for catalytic cracking to obtain propylene, ethylene-rich gas, catalytic cracking slurry oil and a second C4-C5 component;
s5, enabling the steam cracking heavy oil and/or the catalytic cracking slurry oil to enter a residual oil hydrocracking device for hydrocracking treatment to obtain hydrogenated wax oil, and enabling the hydrogenated wax oil to enter the catalytic cracking integrated device for catalytic cracking; wherein the initial boiling point of the steam cracking heavy oil is more than 200 ℃; the distillation range of the catalytic cracking oil slurry is 300-520 ℃.
Optionally, the method further comprises:
feeding the first C4-C5 component and/or the second C4-C5 component to an olefin cracking unit for olefin cracking to obtain ethylene and propylene;
alternatively, the olefin cracking conditions comprise: the reaction temperature is 500-600 ℃, the pressure is 100-500kPa, and the weight space velocity is 3-40h-1。
Optionally, the method further comprises:
prior to performing the first separation, the crude oil is passed into the convection section of the steam cracker 1 for preheating and then mixed with the steam; the temperature of the steam is 300-620 ℃; the temperature of the preheated crude oil is 300-520 ℃.
Optionally, in step S1, the temperature of the flash separator is 300-;
optionally, the steam cracking device further comprises an ultrahigh pressure steam generator for generating pyrolysis steam, wherein the temperature of the pyrolysis steam is 490-650 ℃, and the pressure is 9-15 MPa;
optionally, in step S3, the steam cracking conditions include: the temperature is 800-880 ℃, the retention time is 0.05-0.7s, and the mass ratio of the high-temperature pyrolysis steam to the non-aromatic hydrocarbon component is 0.4-0.8;
alternatively, in step S4, the catalytic cracking conditions include: the reaction pressure is 0.2-0.3MPa, and the temperature of a reaction outlet of the catalytic cracking integrated device is 550-630 ℃;
alternatively, in step S5, the hydrocracking treatment conditions include: the reaction temperature is 400-600 ℃, and the reaction pressure is 10-30 MPa.
Optionally, in step S2, the group composition separating device includes one or more of an adsorption separating device, a solvent extracting device and an extractive distillation device.
Optionally, the method further comprises: the ethylene and propylene obtained in steps S3 and S4 were subjected to collective separation.
Optionally, the crude oil has an API value of 35 to 50 and a sulfur content of 0.01 to 0.5 wt%.
A second aspect of the present disclosure provides a crude oil processing system for producing olefins, the crude oil processing system comprising: a steam cracking device, a flash separator, a group composition separation device, a catalytic cracking integrated device and a residual oil hydrocracking device; the flash separator comprises a first inlet, a light phase outlet, and a heavy phase outlet; the group composition separation device comprises a second inlet, an aromatic hydrocarbon outlet and a non-aromatic hydrocarbon outlet; the steam cracking device comprises a third inlet, a first ethylene outlet, a first propylene outlet, a steam cracking heavy oil outlet and a first C4-C5 component outlet; the catalytic cracking integrated device comprises a fourth inlet, a second ethylene outlet, a second propylene outlet, a catalytic cracking slurry oil outlet and a second C4-C5 component outlet; the residual oil hydrocracking device comprises a fifth inlet and a hydrogenated wax oil outlet;
wherein the first inlet of the flash separator is for introducing high temperature crude oil and steam; the light phase outlet is communicated with the second inlet of the group composition separation device, and the heavy phase outlet is communicated with the fourth inlet of the catalytic cracking integrated device;
the non-aromatic hydrocarbon outlet of the group composition separation device is communicated with the third inlet of the steam cracking device;
the fifth inlet of the residual oil hydrocracking unit is communicated with the steam cracking heavy oil outlet and/or the catalytic cracking slurry oil outlet; and the hydrogenated wax oil outlet is communicated with a fourth inlet of the catalytic cracking integrated device.
Optionally, the system further comprises an olefin cracking unit; the olefin cracking device comprises a sixth inlet, a third ethylene outlet and a third propylene outlet;
the sixth inlet is in communication with the first C4-C5 component outlet and/or the second C4-C5 component outlet.
Optionally, the steam cracker comprises a convection zone and a radiant zone; the convection zone is arranged above the radiation zone; the system further includes a crude oil inlet line having an inlet end for introducing crude oil and an outlet end in communication with the first inlet of the flash separator, and at least a portion of the crude oil inlet line is located within the convection zone of the steam cracking unit, and a steam inlet in communication with the crude oil inlet line between the convection zone and the flash separator.
According to the technical scheme, the crude oil and steam are introduced into the flash separator for first separation, so that a light phase component and a heavy phase component can be obtained, and the separated light phase component and the separated heavy phase component are respectively cracked; according to the method, the light component is subjected to second separation by adopting a group composition separation device, so that an aromatic hydrocarbon component and a non-aromatic hydrocarbon component can be obtained, wherein the non-aromatic hydrocarbon component can be used for preparing components such as ethylene and propylene by steam cracking, and the aromatic hydrocarbon component can further improve the added value of the product; the heavy phase component is catalytically cracked, so that the yield of ethylene and propylene is improved; the method can also be used for returning the cracked heavy oil subjected to steam cracking and the catalytic cracking slurry oil in the cracked product to the catalytic cracking integrated device for further cracking after residual oil hydrocracking, so that the utilization rate of crude oil resources is improved, and the yields of ethylene and propylene are improved. The method realizes the integrated treatment of the light and heavy phase components of the crude oil, improves the resource utilization efficiency, and is beneficial to realizing the flexible optimization of low-carbon olefins, oil products and aromatic hydrocarbon products.
Additional features and advantages of the disclosure will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the disclosure and are incorporated in and constitute a part of this specification, illustrate embodiments of the disclosure and together with the description serve to explain the disclosure without limiting the disclosure. In the drawings:
FIG. 1 is a schematic flow diagram of a crude oil processing system for the production of olefins provided by the present disclosure;
FIG. 2 is a schematic flow diagram of a crude oil processing system employed in a comparative example of the present disclosure.
Description of the reference numerals
1-a steam cracking unit, 2-a flash separator, a group 3-component separation unit, a 4-residual hydrocracking unit, a 5-catalytic cracking integrated unit, a 6-olefin cracking unit, a 7-convection zone, an 8-radiation zone, 101-crude oil, 102-steam, 103-preheated crude oil, 104-a light phase component, 105-a heavy phase component, 106-a non-aromatic hydrocarbon component, 107-an aromatic hydrocarbon component, 113-an aromatic hydrocarbon component, 120-an aromatic hydrocarbon component, 134-an aromatic hydrocarbon component, 110-steam cracked heavy oil, 111-ethylene, 140-ethylene, 130-ethylene-rich gas, 141-propylene, 131-propylene, 114-a first C4-C5 component, 132-a second C4-C5 component, 121-hydrogenated wax oil, 133-catalytic cracking slurry oil; 9-atmospheric and vacuum distillation unit, 10-naphtha hydrogenation unit, 11-aviation kerosene hydrogenation unit, 12-hydrocracking unit, 13-residual oil hydrogenation unit, 14-catalytic cracking unit, 15-reforming extraction unit, 16-gasoline adsorption desulfurization unit, 17-carbon recovery unit, 18-gas separation unit, 19-steam cracking unit, 20-crude oil, 21-naphtha, 22-kerosene, 23-diesel oil and wax oil, 24-residual oil, 25-diesel oil, 26-aviation kerosene, 27-gasoline, 28-light hydrocarbon and light naphtha, 29-second mixed material flow (comprising liquefied gas, pentane oil and raffinate oil), 30-liquefied gas and tail oil, 31-carbon-rich secondary gas, 32-propane and 33-cracked gasoline, 34-pyrolysis fuel oil, 35-aromatic hydrocarbon, 36-propylene, 37-propylene, 38-C4 component, 39-ethylene, 40-pyrolysis C4 component, 41-catalytic diesel oil, 42-catalytic gasoline, 43-dry gas, 44-C3-C4 light hydrocarbon component and 45-hydrogenation naphtha
Detailed Description
The following detailed description of specific embodiments of the present disclosure is provided in connection with the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present disclosure, are given by way of illustration and explanation only, not limitation.
In the present disclosure, unless otherwise specified, the terms "first", "second", "third", and the like are used only for distinguishing different members and do not have actual meanings such as the order of connection before and after the present disclosure. In the present disclosure, the use of directional words such as "upper" and "lower" are upper and lower in the normal use state of the device, and "inner" and "outer" are in terms of the outline of the device.
In a first aspect of the present disclosure, a method for processing crude oil with increased olefin production is provided, and referring to fig. 1, fig. 1 shows a schematic flow diagram of the method for processing crude oil with increased olefin production provided by the present disclosure, comprising the following steps:
s1, enabling the crude oil and the steam to enter a flash separator 2 for first separation, and separating out a light phase component and a heavy phase component;
s2, enabling the light phase component to enter a group composition separation device 3 for second separation, and separating a non-aromatic component and an aromatic component;
s3, enabling the non-aromatic hydrocarbon components to enter a radiation area 8 of a steam cracking device 1 for steam cracking to obtain ethylene, propylene, steam cracking heavy oil and a first C4-C5 component;
s4, allowing the heavy phase component to enter a catalytic cracking integrated device 5 for catalytic cracking to obtain propylene, ethylene-rich gas, catalytic cracking slurry oil and a second C4-C5 component;
s5, enabling the steam cracking heavy oil and/or the catalytic cracking slurry oil to enter a residual oil hydrocracking device 4 for hydrocracking treatment to obtain hydrogenated wax oil, and enabling the hydrogenated wax oil to enter a catalytic cracking integrated device 5 for catalytic cracking; wherein the initial boiling point of the steam cracking heavy oil is more than 200 ℃; the distillation range of the catalytic cracking slurry oil is 300-520 ℃.
According to the method, crude oil and steam are introduced into a flash separator for first separation, so that a light-phase component and a heavy-phase component can be obtained, and the separated light-phase component and the separated heavy-phase component are respectively cracked; according to the method, the light component is subjected to second separation by adopting a group composition separation device, so that an aromatic hydrocarbon component and a non-aromatic hydrocarbon component can be obtained, wherein the non-aromatic hydrocarbon component can be used for preparing components such as ethylene and propylene by steam cracking, and the aromatic hydrocarbon component can further improve the added value of the product; the heavy phase component is catalytically cracked, so that the yield of ethylene and propylene is improved; the method can also be used for returning the cracked heavy oil subjected to steam cracking and the catalytic cracking slurry oil in the cracked product to the catalytic cracking integrated device for further cracking after residual oil hydrocracking, so that the utilization rate of crude oil resources is improved, and the yields of ethylene and propylene are improved. The method realizes the integrated treatment of the light and heavy phase components of the crude oil, improves the resource utilization efficiency, and is beneficial to realizing the flexible optimization of low-carbon olefins, oil products and aromatic hydrocarbon products.
The steam cracking device, the flash separator, the group composition separation device and the catalytic cracking integrated device adopted in the present disclosure are all devices conventionally selected in the field.
In one embodiment, referring to fig. 1, the crude oil processing method provided by the present disclosure may further comprise the steps of:
and (3) leading the first C4-C5 component and/or the second C4-C5 component to an olefin cracking unit 6 for olefin cracking to obtain ethylene and propylene. The C4-C5 component obtained by cracking the light phase component or the heavy phase component is subjected to olefin cracking, so that the utilization rate of raw materials and the yield of ethylene and propylene are further improved.
The olefin cracking unit employed in the present disclosure is a unit of conventional choice in the art.
In a preferred embodiment, the conditions for olefin cracking comprise: the reaction temperature is 500-600 ℃, the pressure is 100-500kPa, and the weight space velocity is 3-40h-1The olefin cracking catalyst may be selected from those known in the art.
In one embodiment, referring to fig. 1, the crude oil processing method provided by the present disclosure further comprises: the crude oil is preheated in the convection zone 7 of the steam cracker 1 before being subjected to the first separation and then mixed with steam; the temperature of the steam is 300-620 ℃; the temperature of the preheated crude oil is 300-520 ℃. The convection zone that this openly introduces crude oil steam cracking device preheats, make full use of the heat of device self, reduced the energy loss.
In one embodiment, the temperature of the flash separator 2 in step S1 is 300-.
In one embodiment, the steam cracking apparatus 1 further comprises an ultrahigh pressure steam generator, wherein the temperature of the high temperature cracking steam generated by the ultrahigh pressure steam generator is 490-650 ℃, and the pressure is 9-15 MPa.
In one embodiment, in step S3, the steam cracking conditions include: the temperature is 800-880 ℃, the retention time is 0.05-0.7s, and the mass ratio of the pyrolysis steam to the non-aromatic components is 0.4-0.8.
In one embodiment, in step S4, the conditions for catalytic cracking include: the reaction pressure is 0.2-0.3MPa, the reaction outlet temperature of the catalytic cracking integrated device 5 is 550-.
In one embodiment, the hydrocracking process conditions in step S5 include: the reaction temperature is 400-600 ℃, the reaction pressure is 10-30MPa, and the hydrocracking catalyst can be selected from the catalysts known in the field.
In one embodiment, in step S2, the group composition separating device 3 includes one or more of an adsorption separating device, a solvent extracting device, and an extractive distillation device.
In a preferred embodiment, the aromatic hydrocarbon component separated by the group composition separating means may be produced in the form of a product such as an aromatic hydrocarbon or a solvent oil, to enhance the added value of the product.
In a preferred embodiment, the crude oil processing method provided by the present disclosure further comprises: the ethylene and the propylene obtained in the steps S3 and S4 are separated in a centralized way, so that the separation cost is reduced.
The separation apparatus employed in the present disclosure to perform the focused separation is an apparatus of conventional choice in the art.
In one embodiment, the crude oil has an API value of 35 to 50 and a sulfur content of 0.01 to 0.15 wt%.
A second aspect of the present disclosure provides a crude oil processing system for the production of olefins, as shown in fig. 1, the system comprising: a steam cracking device 1, a flash separator 2, a group composition separation device 3, a catalytic cracking integrated device 5 and a residual oil hydrocracking device 4; the flash separator 2 comprises a first inlet, a light phase outlet and a heavy phase outlet; the group composition separation device 3 comprises a second inlet, an aromatic hydrocarbon outlet and a non-aromatic hydrocarbon outlet; the steam cracking device 1 comprises a third inlet, a first ethylene outlet, a first propylene outlet, a steam cracking heavy oil outlet and a first C4-C5 component outlet; the catalytic cracking integrated device 5 comprises a fourth inlet, a second ethylene outlet, a second propylene outlet, a catalytic cracking slurry oil outlet and a second C4-C5 component outlet; the residual oil hydrocracking device 4 comprises a fifth inlet and a hydrogenated wax oil outlet;
wherein the first inlet of the flash separator 2 is for introducing high temperature crude oil and steam; the light phase outlet is communicated with the second inlet of the group composition separation device 3, and the heavy phase outlet is communicated with the fourth inlet of the catalytic cracking integrated device 5;
the non-aromatic hydrocarbon outlet of the group composition separation device 3 is communicated with the third inlet of the steam cracking device 1;
a fifth inlet of the residual oil hydrocracking device 4 is communicated with a steam cracking heavy oil outlet and/or a catalytic cracking slurry oil outlet; the hydrogenated wax oil outlet is communicated with a fourth inlet of the catalytic cracking integrated device 5.
In one embodiment, the system further comprises an olefin cracking unit 6; the olefin cracking device 6 comprises a sixth inlet, a third ethylene outlet and a third propylene outlet;
the sixth inlet is in communication with the first C4-C5 component outlet and/or the second C4-C5 component outlet.
In a preferred embodiment, the steam cracking unit 1 comprises a convection zone 7 and a radiant zone 8; the convection zone 7 is arranged above the radiation zone 8; the system further comprises a crude oil inlet line having an inlet end for introducing crude oil and an outlet end in communication with the first inlet of the flash separator 2, and at least a portion of the crude oil inlet line is located within the convection zone 7 of the steam cracking unit 1, and a steam inlet in communication with the crude oil inlet line between the convection zone 7 and the flash separator 2.
In one embodiment, the integrated catalytic cracking apparatus 5 may be a riser reactor.
In a specific embodiment, the steam cracking device 1 is further provided with an ultrahigh pressure steam generator, which is arranged below the radiation zone 8 and is used for generating high-temperature steam to perform steam cracking on the light-phase component; optionally, the temperature of the ultrahigh pressure steam generator is 490-650 ℃, and the pressure is 9-15 MPa.
The present disclosure will be further illustrated with reference to the following examples.
The following example 1 used sauter ultra light crude oil (0.05% sulfur) of API40 as crude oil, example 2 used tahe northward crude oil (0.04% sulfur) of API46.5 as crude oil, and comparative example 1 used sauter heavy mixed crude oil (0.1% sulfur) of API30 as crude oil.
Example 1
The ethylene and the propylene are produced according to the crude oil processing system for producing more olefin shown in the figure 1, and the specific flow is as follows:
s1, crude oil 101 enters a convection zone 7 of a steam cracking device 1 to be preheated, steam 102 (temperature 425 ℃ and pressure 1000kPa) and preheated crude oil (temperature 450 ℃ and pressure 620kPa) are mixed (the flow ratio of the steam to the crude oil is 0.5), and the mixture enters a flash separator 2 to be subjected to first separation to obtain a light phase component 104 and a heavy phase component 105, wherein the temperature in the flash separator is 440 ℃ and the pressure in the flash separator is 620 kPa.
S2, the light phase component 104 enters a group composition separation device 3 for second separation to separate a non-aromatic hydrocarbon component 106 and an aromatic hydrocarbon component 107, the group composition separation device is specifically an adsorption separation device, and the second separation operation conditions comprise 1MPa and 60 ℃.
S3, allowing the heavy phase component 105 to enter a catalytic cracking integrated device 5 for catalytic cracking to produce ethylene-rich gas 130 (led out through a second ethylene outlet), propylene 131 (led out through a second propylene outlet), an aromatic hydrocarbon component 134, catalytic cracking slurry oil 133 and a second C4-C5 component 132; wherein the reaction pressure is 0.25MPa, the outlet temperature is 610 ℃, and the main chemical component of the catalytic cracking catalyst is alumina.
S4, introducing the non-aromatic hydrocarbon component 106 separated by the group composition separation device 3 into the radiation zone 8 of the steam cracking device 1 to produce ethylene 111 (led out through a first ethylene outlet), propylene 112 (led out through a first propylene outlet), an aromatic hydrocarbon component 113, steam cracking heavy oil 110 and a first C4-C5 component 114; in the steam cracking process, the temperature is 830 ℃, and the retention time is 0.2 s.
S5, introducing the steam cracked heavy oil 110 and the catalytic cracked slurry oil 133 (the initial boiling point of the steam cracked heavy oil is more than 200 ℃, the distillation range of the catalytic cracked slurry oil is 300-520 ℃) into a residual oil hydrocracking device 4 for hydrocracking treatment to produce an aromatic hydrocarbon component 120 and a hydrogenated wax oil 121, wherein the hydrocracking temperature is 420 ℃, the pressure is 15MPa, and the hydrocracking catalyst is an oil-soluble molybdenum-based catalyst.
S6, introducing the hydrogenated wax oil 121 obtained in the step S5 into a catalytic cracking integrated device 5 for further cracking.
S7, introducing the first C4-C5 component and the second C4-C5 component produced in the steps S3 and S4 into an olefin cracking device 6 for further cracking to produce ethylene 140 (led out through a third ethylene outlet) and propylene 141 (led out through a third propylene outlet), wherein the reaction temperature in the olefin cracking device is 520 ℃, the pressure is 200kPa, and the space velocity is 15h-1. The olefin cracking catalyst is a silica/alumina system. The products obtained in example 1 and their indices are listed in table 1 below.
Example 2
Referring to the process flow used in example 1, the only difference from example 1 is that the crude oil used was API46.5 Tahe northward crude oil (sulfur content 0.04%). The products obtained in example 2 and their indices are listed in table 1 below.
Comparative example 1
The olefin production process, shown in FIG. 2, which is conventionally employed in the art, specifically includes the following steps:
(1) the crude oil 20 is often subjected to vacuum distillation 9 to separate naphtha 21, kerosene 22, diesel and wax oil 23 and residual oil 24.
(2) Obtaining a first mixture flow and light hydrocarbon and light naphtha 28 after naphtha 21 is subjected to hydrotreating by a naphtha hydrogenation device 10, and sending the first mixture flow to a reforming extraction device 15 to produce aromatic hydrocarbon 35, gasoline 27 and a second mixture flow 29 (the second mixture flow 29 comprises liquefied gas, pentane oil and raffinate oil); the light hydrocarbon and light naphtha 28 are introduced into the steam cracker 19 for further cracking.
(3) The kerosene 22 enters the aviation kerosene hydrogenation device 11 for hydrogenation treatment to obtain an aviation kerosene product 26.
(4) Sending the diesel oil and the wax oil 23 into a hydrocracking device 12 for processing to produce hydrogenated naphtha 45, aviation kerosene 26, diesel oil 25, liquefied gas and tail oil 30, wherein the hydrocracking reaction temperature is 420 ℃, and the reaction pressure is 17 MPa; the liquefied gas and the tail oil 30 are sent to a steam cracking unit 19 to be cracked, and the hydrogenated naphtha 45 is sent to a reforming extraction unit 15 to be processed.
(5) The residual oil 24 is sent to a residual oil hydrogenation device 13 for hydrogenation treatment, wherein the hydrogenation catalyst is a nickel-molybdenum system catalyst, the temperature is 400 ℃, and the pressure is 17.5 MPa; sending the product obtained by hydrotreating to a catalytic cracking device 14 for catalytic cracking to produce catalytic gasoline 42, catalytic diesel oil 41, dry gas 43 and C3-C4 light hydrocarbon components 44; wherein the catalytic cracking reaction pressure is 0.25MPa, the outlet temperature is 610 ℃, and the main chemical component of the catalytic cracking catalyst is alumina.
(6) Sending the catalytic diesel oil 41 obtained in the step (5) to a hydrocracking unit 12 for treatment; sending the catalytic gasoline 42 to a gasoline adsorption desulfurization device 16 to obtain gasoline 27;
the dry gas 43 is treated by a carbon dioxide recovery device 17 to obtain carbon-rich gas 31; separating the C3-C4 light hydrocarbon components 44 into propane 32, propylene 36 and C4 components 38 through the gas separation device 18; the propane 32 and the carbon-rich second gas 31 are sent to the steam cracker 19 for further cracking.
(7) The steam cracking device 19 is adopted to produce ethylene 39, propylene 37, cracked C4 component 40, cracked gasoline 33 and cracked fuel oil 34. Wherein the steam cracking conditions comprise: the temperature is 800 ℃ and 830 ℃, and the retention time is 0.05-0.2 s. The products obtained in comparative example 1 and their indices are listed in table 1 below.
The raw material and product specifications of the above examples and comparative examples are listed in table 1 below, under ethylene production conditions of 150 million tons/year:
TABLE 1
As can be seen from the above table, the crude oil amount required for the crude oil processing method provided in example 1 of the present disclosure is 680 ten thousand tons/year under the same ethylene yield; the crude oil amount required by the crude oil processing method provided by the embodiment 2 of the disclosure is 520 ten thousand tons/year; whereas the crude oil quantity required with the crude oil processing method provided in comparative example 1 is up to 1200 ten thousand tons/year. The crude oil processing method provided by the present disclosure therefore significantly improves the utilization of crude oil.
Further, in terms of product structure, compared with comparative example 1, the yield of ethylene, propylene and carbon tetraolefin produced by unit crude oil of example 1 and example 2 of the present disclosure is high, the oil yield is low, and the method is more suitable for refining enterprises aiming at high production of low carbon olefin.
In addition, in the aspect of investment benefit, the embodiment has short processing route and small device scale, so that the construction investment of the whole plant can be greatly saved compared with the proportion 1. The crude oil processing method and the crude oil processing system can obtain better economic benefits.
The preferred embodiments of the present disclosure are described in detail with reference to the accompanying drawings, however, the present disclosure is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present disclosure within the technical idea of the present disclosure, and these simple modifications all belong to the protection scope of the present disclosure.
It should be noted that the various features described in the above embodiments may be combined in any suitable manner without departing from the scope of the invention. In order to avoid unnecessary repetition, various possible combinations will not be separately described in this disclosure.
In addition, any combination of various embodiments of the present disclosure may be made, and the same should be considered as the disclosure of the present disclosure, as long as it does not depart from the spirit of the present disclosure.
Claims (10)
1. A method for processing crude oil with high olefin yield is characterized by comprising the following steps:
s1, enabling the crude oil and the steam to enter a flash separator (2) for first separation, and separating out a light phase component and a heavy phase component;
s2, enabling the light phase component to enter a group composition separation device (3) for second separation, and separating a non-aromatic component and an aromatic component;
s3, feeding the non-aromatic hydrocarbon components into a radiation area (8) of a steam cracking device (1) for steam cracking to obtain ethylene, propylene, steam cracking heavy oil and a first C4-C5 component;
s4, enabling the heavy phase component to enter a catalytic cracking integrated device (5) for catalytic cracking to obtain propylene, ethylene-rich gas, catalytic cracking slurry oil and a second C4-C5 component;
s5, feeding the steam cracking heavy oil and/or the catalytic cracking slurry oil into a residual oil hydrocracking device (4) for hydrocracking treatment to obtain hydrogenated wax oil, and feeding the hydrogenated wax oil into the catalytic cracking integrated device (5) for catalytic cracking; wherein the initial boiling point of the steam cracking heavy oil is more than 200 ℃; the distillation range of the catalytic cracking oil slurry is 300-520 ℃.
2. The crude oil processing method as claimed in claim 1, further comprising:
feeding the first C4-C5 component and/or the second C4-C5 component to an olefin cracking unit (6) for olefin cracking to obtain ethylene and propylene;
alternatively, the olefin cracking conditions comprise: the reaction temperature is 500-600 ℃, the pressure is 100-500kPa, and the weight space velocity is 3-40h-1。
3. The crude oil processing method as claimed in claim 1, further comprising:
prior to performing the first separation, the crude oil is passed into a convection zone (7) of the steam cracking unit (1) for preheating and then mixed with the steam; the temperature of the steam is 300-620 ℃; the temperature of the preheated crude oil is 300-520 ℃.
4. The crude oil processing method according to claim 1, characterized in that in step S1, the temperature of the flash separator (2) is 300-520 ℃, preferably 400-480 ℃;
optionally, the steam cracking device (1) further comprises an ultrahigh pressure steam generator, wherein the temperature of the high temperature cracking steam generated by the ultrahigh pressure steam generator is 490-650 ℃, and the pressure is 9-15 MPa;
optionally, in step S3, the steam cracking conditions include: the temperature is 800-880 ℃, the retention time is 0.05-0.7s, and the mass ratio of the high-temperature pyrolysis steam to the non-aromatic hydrocarbon component is 0.4-0.8;
alternatively, in step S4, the catalytic cracking conditions include: the reaction pressure is 0.2-0.3MPa, and the reaction outlet temperature of the catalytic cracking integrated device (5) is 550-630 ℃;
alternatively, in step S5, the hydrocracking treatment conditions include: the reaction temperature is 400 ℃ and 600 ℃, and the reaction pressure is 10-30 MPa.
5. The crude oil processing method according to claim 1, wherein in step S2, the group composition separating means (3) comprises one or more of an adsorption separating means, a solvent extracting means, and an extractive distillation means.
6. The crude oil processing method as claimed in claim 1, further comprising: the ethylene and propylene obtained in steps S3 and S4 were collectively separated.
7. The crude oil processing method as claimed in claim 1, characterized in that the crude oil has an API value of 35 to 50 and a sulphur content of 0.01 to 0.5 wt.%.
8. A crude oil processing system for producing a high amount of olefins, the crude oil processing system comprising: a steam cracking device (1), a flash separator (2), a group composition separation device (3), a catalytic cracking integrated device (5) and a residual oil hydrocracking device (4); the flash separator (2) comprises a first inlet, a light phase outlet and a heavy phase outlet; the group composition separation device (3) comprises a second inlet, an aromatic hydrocarbon outlet and a non-aromatic hydrocarbon outlet; the steam cracking device (1) comprises a third inlet, a first ethylene outlet, a first propylene outlet, a steam cracking heavy oil outlet and a first C4-C5 component outlet; the catalytic cracking integrated device (5) comprises a fourth inlet, a second ethylene outlet, a second propylene outlet, a catalytic cracking slurry oil outlet and a second C4-C5 component outlet; the residual oil hydrocracking device (4) comprises a fifth inlet and a hydrogenated wax oil outlet;
wherein a first inlet of the flash separator (2) is for introducing high temperature crude oil and steam; the light phase outlet is communicated with the second inlet of the group composition separation device (3), and the heavy phase outlet is communicated with the fourth inlet of the catalytic cracking integrated device (5);
the non-aromatic hydrocarbon outlet of the group composition separation device (3) is communicated with the third inlet of the steam cracking device (1);
the fifth inlet of the residual oil hydrocracking device (4) is communicated with the steam cracking heavy oil outlet and/or the catalytic cracking slurry oil outlet; the hydrogenated wax oil outlet is communicated with a fourth inlet of the catalytic cracking integrated device (5).
9. The system of claim 8, further comprising an olefin cracking unit (6); the olefin cracking device (6) comprises a sixth inlet, a third ethylene outlet and a third propylene outlet;
the sixth inlet is in communication with the first C4-C5 component outlet and/or the second C4-C5 component outlet.
10. The system according to claim 8, characterized in that the steam cracking device (1) comprises a convection zone (7) and a radiation zone (8); the convection zone (7) is arranged above the radiation zone (8); the system further comprises a crude oil inlet line having an inlet end for introducing crude oil and an outlet end communicating with the first inlet of the flash separator (2), and at least a portion of the crude oil inlet line being located within the convection zone (7) of the steam cracking unit (1), and a steam inlet communicating with the crude oil inlet line between the convection zone (7) and the flash separator (2).
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