Gas-liquid separation device and use thereof in preparation of olefin by steam cracking

Abstract

The present invention relates to a gas-liquid separation device and the use thereof in the preparation of olefin by steam cracking. A method for preparing olefin by steam cracking of the present invention comprises the following steps: heating heavy hydrocarbon to obtain a gas-liquid mixture; conveying the gas-liquid mixture into a gas-liquid separation device for gas-liquid separation so as to obtain gas-phase materials and liquid-phase materials, wherein the gas-liquid separation device comprises an inner cavity, a liquid-phase outlet, a gas-phase outlet, one or more baffles, which divide at least the middle of the inner cavity into n separation chambers in the direction of the central axis of the inner cavity, a gas-liquid separation feeding device, and gas-liquid separation components, which are respectively arranged inside the n separation chambers and are configured to be capable of respectively performing gas-liquid separation in the n separation chambers, so as to obtain the corresponding n gas-phase materials and n liquid-phase materials; and performing steam cracking on at least one of the n gas-phase materials or the combined gas-phase materials to obtain a cracking product containing olefin. The gas-liquid separation device of the present invention has the characteristics of long-period operation, etc.

Description

A gas-liquid separation device and its application in steam cracking to produce olefins Technical Field

[0001] The present invention relates to the technical field of steam cracking, and more particularly to a gas-liquid separation device and its application in the production of olefins by steam cracking. Background Art

[0002] Currently, global oil demand is declining annually with the development of new energy sources, while refining capacity is currently in excess. Therefore, research on efficient and streamlined crude oil utilization, reducing investment and energy consumption in crude oil utilization equipment, and improving equipment economics have become a common concern in the global refining and chemical industry.

[0003] To this end, researchers at home and abroad have developed flash evaporation methods, applying crude oil to crude oil processing and steam cracking. The boiling point of a substance increases with increasing pressure; conversely, the lower the pressure, the lower the boiling point. Flash evaporation works by reducing the pressure on a high-pressure, high-temperature fluid to lower its boiling point. This process, when the high-temperature liquid nears its boiling point under high pressure is reduced in pressure, partially vaporizes after absorbing its own energy, and forms a new vapor-liquid equilibrium. This means the fluid temperature is higher than its boiling point at that pressure, causing it to rapidly boil and vaporize, and the two phases to separate.

[0004] Because conventional flash tanks have extremely low separation efficiency and are bulky, occupying a lot of space, researchers at home and abroad have made significant progress through continuous in-depth research. Currently, crude oil flash treatment focuses on the following aspects: optimizing the vacuum pumping system to increase the vacuum level at the top of the vessel; using new, efficient packing and direct contact heat transfer methods to reduce the total pressure drop in the vessel and maintain a high vacuum level in the flash section; optimizing the design and operation of the wash section and strengthening the fractionation concept in the wash section; developing new, efficient gas and liquid distributors; and adopting enhanced crude oil distillation methods.

[0005] CN03815733.0 discloses a method for steam cracking heavy hydrocarbon feedstocks. The feedstock is prepared by mixing preheated heavy hydrocarbons with water and dilution steam to form a mixed stream, which is then passed through a flash tank to separate the vapor phase from the liquid phase. The vapor phase then passes through a separator to further remove non-volatiles, and the resulting vapor product enters a cracking furnace for cracking.

[0006] Summary of the Invention

[0007] The object of the present invention is to provide a gas-liquid separation device and its application in the production of olefins by steam cracking. By means of a chamber division means of the gas-liquid separation device, fine control of each chamber can be achieved. The purpose is to solve the problems in the prior art of the continuous enlargement of the scale of ethylene cracking furnaces, the increasing number of feed groups, and the continuous increase in feed amount. In particular, the existence of grouping and feeding different raw materials into different furnace chambers leads to severe production fluctuations, resulting in low gas-liquid separation efficiency during operation, poor flash evaporation effect, and difficulty in long-term operation.

[0008] Specifically, the present invention relates to the following aspects.

[0009] In a first aspect, the present invention relates to a method for producing olefins by steam cracking, comprising the following steps:

[0010] 1) Heating heavy hydrocarbons to obtain a gas-liquid mixture,

[0011] 2) transporting the gas-liquid mixture into a gas-liquid separation device for gas-liquid separation to obtain a gas phase material and a liquid phase material, wherein the gas-liquid separation device comprises:

[0012] an inner cavity comprising a top, an upper portion, a middle portion, a lower portion and a bottom portion,

[0013] a liquid phase outlet, which is located at the bottom of the inner cavity and is configured to output the liquid phase material from the gas-liquid separation device,

[0014] a gas phase outlet, which is located at the top of the inner cavity and is configured to output the gas phase material from the gas-liquid separation device,

[0015] One or more baffles, which divide at least the middle part (preferably the upper part, the middle part and the lower part) of the inner cavity into n separation chambers along the central axis of the inner cavity, wherein each of the separation chambers includes an upper part, a middle part and a lower part, and n is an integer selected from 2-16 (preferably an integer selected from 4-8),

[0016] a gas-liquid separation feeding device (preferably a gas-liquid separation feeding distributor), which is respectively arranged inside the n separation chambers and is configured to be able to transport the gas-liquid mixture into the n separation chambers respectively, and

[0017] Gas-liquid separation components are respectively arranged inside the n separation chambers and are configured to perform the gas-liquid separation in the n separation chambers to obtain corresponding n gas-phase materials and n liquid-phase materials.

[0018] 3) optionally, combining at least two of the n gas phase feeds together to form a comprehensive gas phase feed, and optionally, combining at least two (preferably all) of the n liquid phase feeds together to form a comprehensive liquid phase feed,

[0019] 4) steam cracking at least one (preferably all) of the n gaseous materials or the comprehensive gaseous materials to obtain a cracking product containing the olefin.

[0020] In a second aspect, the present invention relates to a gas-liquid separation device comprising:

[0021] an inner cavity comprising a top, an upper portion, a middle portion, a lower portion and a bottom portion,

[0022] a liquid phase outlet, which is located at the bottom of the inner cavity,

[0023] a gas phase outlet, which is located at the top of the inner cavity,

[0024] One or more baffles, which divide at least the middle part (preferably the upper part, the middle part and the lower part) of the inner cavity into n separation chambers along the central axis of the inner cavity, wherein each of the separation chambers includes an upper part, a middle part and a lower part,

[0025] A gas-liquid separation feeding device (preferably a gas-liquid separation feeding distributor) is respectively arranged inside the n separation chambers,

[0026] Gas-liquid separation components are configured to achieve a gas-liquid separation function and are disposed inside the n separation chambers,

[0027] In which, the gas-liquid separation component arranged inside the mth separation chamber is different from the gas-liquid separation component arranged inside the ith separation chamber, n is an integer selected from 2-16 (preferably an integer selected from 4-8), m and i are different, and each is independently selected from an integer from 1 to n.

[0028] In a third aspect, the present invention relates to a gas-liquid separation method, comprising the step of transporting the gas-liquid separation feed through a gas-liquid separation feed device (preferably a gas-liquid separation feed distributor) into the gas-liquid separation device described in any of the preceding or following aspects to perform gas-liquid separation.

[0029] Technical Effects

[0030] The present invention uses baffles to separate the flash separation equipment into multiple, side-by-side separation chambers. After separation, the high-temperature vapor-hydrocarbon mixture entering the separation chambers is directly fed to downstream equipment through the gas phase outlet of the separation chambers. As the scale of a single cracking furnace increases, and when grouped or divided furnace feeding is used, the operating parameters of each separation chamber are precisely controlled to maintain a fluctuation range of performance indicators such as the vaporization rate within the separation chamber below 5%. Combined with the temperature control of the radiant section tube outlet of the cracking furnace, this ensures that the feedstock group is in the optimal steam cracking state, thereby ensuring smooth operation of the cracking furnace, achieving optimal product yield and a long coke cleaning cycle, further reducing operating and maintenance costs and improving economic benefits. Furthermore, by injecting a cooling aid, a washing aid, and an optional stripping aid, the present invention can, on the one hand, reduce the content of heavy fractions and impurities such as colloids in the gas phase, thereby improving gas-liquid separation efficiency and preventing coking in the radiant section, thereby extending the coke cleaning cycle of the cracking furnace; and, on the other hand, reduce the content of light components in the liquid phase. Injecting a separation or stripping agent can maximize the stripping of light components from the liquid phase, thereby maximizing light component recovery. Injecting a cooling agent can control the vaporization rate and reduce the carryover of heavy components, while increasing the liquid flow rate to enhance the separation efficiency of the trays. Furthermore, the installation of a hydrocyclone and trays in each separation chamber can improve gas-liquid separation efficiency and flash evaporation, further reducing the carryover of heavy components and impurities such as colloids, preventing them from coking in the radiant section, and thus further extending the decoking cycle of the cracking furnace. BRIEF DESCRIPTION OF THE DRAWINGS

[0031] FIG1 is a schematic diagram of a heavy hydrocarbon steam cracking system according to the present invention (first embodiment series).

[0032] FIG2 is a schematic diagram of a heavy hydrocarbon steam cracking system according to the present invention (first embodiment series).

[0033] FIG3 is a front view of the gas-liquid separation device used in Comparative Example 1.

[0034] FIG4 is a top view of the gas-liquid separation device of the present invention (first embodiment series).

[0035] FIG5 is a schematic diagram of a gas-liquid separation device according to the present invention (second embodiment series).

[0036] FIG6 is a top view of the gas-liquid separation device of the present invention (second embodiment series).

[0037] FIG7 is a schematic diagram of a gas-liquid separation device in the prior art.

[0038] Description of Reference Numerals

[0039] In Figures 1 to 4, 1, gas phase outlet; 2, gas-hydrocarbon mixture inlet; 3, liquid phase outlet; 4, cooling / washing aid inlet; 5, stripping aid inlet; 6, cyclone separator; 7, tower plate; 8, sealing cover plate; 9, baffle; 10, liquid storage space; a, raw material pipeline; b, steam pipeline; b1, primary steam pipeline; b2, secondary steam pipeline; c, cooling / washing aid pipeline; d, stripping aid pipeline.

[0040] In Figures 5 to 7, 1. Vertical shell; 2. Diversion distribution module; 3. Tower tray; 4. Inlet steam distributor; 5. Cyclone separator group; 6. Downcomer group; 7. Horizontal partition plate; 8. Overflow collection chamber; 9. Liquid collecting area; 10. Baffle; 11. Manifold; 12. Gas-hydrocarbon mixture inlet; 13. Cooling / washing aid inlet; 14. Stripping aid inlet; 15. Gas phase outlet; 16. Liquid phase outlet. DETAILED DESCRIPTION

[0041] The specific embodiments of the present invention are described in detail below. However, it should be noted that the protection scope of the present invention is not limited by these specific embodiments, but is determined by the claims in the appendix.

[0042] All publications, patent applications, patents, and other references mentioned in this specification are incorporated herein by reference. Unless otherwise defined, all technical and scientific terms used in this specification have the meanings commonly understood by those skilled in the art. In the event of conflict, the definitions in this specification will prevail.

[0043] When this specification uses the prefix "well known to those skilled in the art", "prior art" or similar terms to introduce materials, substances, methods, steps, devices or components, the objects introduced by the prefix include those conventionally used in the art when the present invention was proposed, but also include those that are not commonly used at present but will become generally recognized in the art to be suitable for similar purposes.

[0044] In the context of the present invention, all numerical values ​​for parameters (eg, amounts or conditions) are to be understood as being modified in all instances by the term "about," regardless of whether "about" actually appears before the numerical value.

[0045] In the context of the present invention, “substantially” means that deviations that are acceptable or reasonable to those skilled in the art are allowed, such as deviations within ±2%, within ±1%, within ±0.5% or within ±0.1%.

[0046] Unless expressly stated otherwise, throughout the specification and claims, the term “comprise” or variations such as “include” or “comprising” will be understood to include the stated elements or components but not to exclude other elements or components.

[0047] In the context of the present invention, unless otherwise specified, directional words such as "upper" and "lower" generally refer to the upper and lower parts of the device in normal use, for example, with reference to the drawing direction of Figure 1, and "inside" and "outside" refer to the outline of the device. More specifically, unless otherwise specified, directional words such as top, upper, middle, lower and bottom generally refer to the normal use state of the device. For example, the top generally refers to the area 10% or less from the top of the device downward along the central axis of the device, more particularly refers to the top head area, the middle generally refers to the area located near half of the height of the device along the central axis of the device, the bottom generally refers to the area 10% or less from the bottom of the device upward along the central axis of the device, more particularly refers to the bottom head area, and the upper and lower parts generally refer to the area between the top and the middle and the area between the middle and the bottom, respectively. However, it will be apparent to those skilled in the art that the present invention is not limited to this.

[0048] In the context of the present invention, the terms "first" and "second" are used for descriptive purposes only and should not be understood to indicate or imply relative importance or implicitly specify the number of the technical features indicated. Therefore, features specified as "first" and "second" may explicitly or implicitly include one or more of the features. In the description of this disclosure, "plurality" means two or more, unless otherwise specifically defined.

[0049] In the context of the present invention, the terms "primary dilution steam", "secondary dilution steam" and the like are only used to distinguish the steam introduced in different steps, and do not contain any actual meaning such as the properties of the steam itself.

[0050] In the context of the present invention, unless otherwise specified, the various devices used in the present invention may use structures conventionally selected in the art without particular limitation.

[0051] In the context of the present invention, heavy hydrocarbons refer to mixed hydrocarbons with a broad distillation range, typically with an end-point above 540°C, for example, an initial distillation point of 15°C and an end-point of approximately 750°C. Specifically, these heavy hydrocarbons can be selected from one or more of the following feedstocks: paraffinic crude oil, intermediate crude oil, naphthenic crude oil, condensate, and refinery products. Examples of refinery products include gasoline, kerosene, diesel, tail oil, fuel oil, and reformate, which are processed in refinery units such as atmospheric and vacuum distillation, reforming, catalytic, and coking.

[0052] In the context of the present invention, the initial boiling point, final boiling point and distillation range are measured by atmospheric and vacuum distillation of crude oil, wherein the atmospheric distillation analysis method adopts ASTM D-2892, and the vacuum distillation analysis method adopts ASTM D-5236.

[0053] In the context of the present invention, API refers to specific gravity index, and its analysis method adopts ASTM D-2320.

[0054] In the context of the present invention, non-volatile components specifically refer to components with a final boiling point exceeding 590° C., and the analysis method for non-volatile components adopts ASTM D6352.

[0055] In the context of the present invention, the gasification rate refers to the mass percentage of gas phase material (excluding steam) to the total amount of feed (excluding steam).

[0056] Unless otherwise specified, all percentages, parts, ratios, etc. mentioned in this specification are based on weight and pressure is gauge pressure.

[0057] In the context of the present invention, any two or more embodiments or aspects of the present invention may be arbitrarily combined, and the technical solutions thus formed belong to part of the original disclosure of this specification and also fall within the scope of protection of the present invention.

[0058] According to one embodiment of the present invention, a method for producing olefins by steam cracking is provided, particularly a method for producing ethylene by steam cracking heavy hydrocarbons. Unless otherwise specified in the present invention, those skilled in the art may directly apply relevant information commonly known in the art as needed, and no further details are provided herein.

[0059] According to one embodiment of the present invention, a gas-liquid separation device is provided, comprising: an inner chamber comprising a top, an upper portion, a middle portion, a lower portion, and a bottom portion; a liquid phase outlet located at the bottom portion of the inner chamber; and a gas phase outlet located at the top portion of the inner chamber. In the context of this specification, the method for producing olefins by steam cracking and the gas-liquid separation device are described together without distinguishing between them. Therefore, unless otherwise specified, the specific description of the method for producing olefins by steam cracking also applies to the gas-liquid separation device, and vice versa.

[0060] According to one embodiment of the present invention, the inner cavity is surrounded by a vertical shell, and the vertical shell is a cylindrical shell, as shown in the accompanying drawings of the present invention.

[0061] According to one embodiment of the present invention, the method for producing olefins by steam cracking includes step 1): heating heavy hydrocarbons to obtain a gas-liquid mixture.

[0062] According to one embodiment of the present invention, in step 1), the heavy hydrocarbons are heated to 100-400° C. (preferably 200-370° C.). According to the present invention, the heating can be carried out in any manner conventionally known in the art without particular limitation, but is generally carried out in the convection section of the cracking furnace.

[0063] According to one embodiment of the present invention, the final boiling point temperature of the heavy hydrocarbon is above 540°C (preferably, the initial boiling point temperature is 15°C and the final boiling point temperature is above 750°C). Preferably, the API value of the heavy hydrocarbon is not less than 32 (preferably above 38). For example, the heavy hydrocarbon is selected from at least one of paraffinic crude oil, intermediate crude oil, naphthenic crude oil, condensate oil, and refined products.

[0064] According to one embodiment of the present invention, the method for producing olefins by steam cracking comprises step 2): transporting the gas-liquid mixture into a gas-liquid separation device for gas-liquid separation.

[0065] According to one embodiment of the present invention, the gas-liquid separation device includes: an inner cavity, which includes a top, an upper part, a middle part, a lower part and a bottom part, a liquid phase outlet, which is located at the bottom of the inner cavity and is configured to be able to output the liquid phase material from the gas-liquid separation device, and a gas phase outlet, which is located at the top of the inner cavity and is configured to be able to output the gas phase material from the gas-liquid separation device.

[0066] According to one embodiment of the present invention, the gas-liquid separation device further includes one or more baffles that separate at least the middle portion (preferably the upper portion, the middle portion, and the lower portion) of the inner cavity into n separation chambers along the central axis of the inner cavity. Here, each of the separation chambers includes an upper portion, a middle portion, and a lower portion.

[0067] According to one embodiment of the present invention, n is an integer selected from 2-16 (preferably an integer selected from 4-8). The inventors of the present invention have discovered that different numbers of separation chambers can be provided depending on the number of feed groups in the cracking furnace. The number of separation chambers can be the same as the number of feed groups or a multiple of the number of feed groups. By changing the operating parameters of the separation chamber, performance indicators such as the gasification rate of the separation chamber can be precisely controlled to ensure that the gasification rate fluctuates within a range of less than 5% (preferably less than 2%, more preferably less than 1% or less than 0.5%), thereby ensuring that the group of raw materials is in an optimal steam cracking state.

[0068] According to one embodiment of the present invention, in the n separation chambers, the operating temperatures for the gas-liquid separation are the same or different, and are each independently 100-400°C (preferably 200-370°C). The operating pressures for the gas-liquid separation are the same or different, and are each independently 0.4-0.7 MPaG. The inventors of the present invention have discovered that by independently adjusting the operating temperature or operating pressure of each separation chamber based on the properties of the components entering the set of separation chambers, the target gasification rate requirement is achieved, with a fluctuation range of less than 5% (preferably less than 2%, more preferably less than 1% or less than 0.5%), ensuring that the set of feedstocks is in an optimal steam cracking state.

[0069] According to one embodiment of the present invention, the gas-liquid separation device further comprises a gas-liquid separation feed device (preferably a gas-liquid separation feed distributor), which is respectively disposed inside the n separation chambers and is configured to be able to transport the gas-liquid mixture into the n separation chambers. In the context of the present invention, the gas-liquid separation feed is sometimes also referred to as a vapor-hydrocarbon mixture.

[0070] According to one embodiment of the present invention, the volumes of the n separation chambers are the same or different, and can be evenly distributed among each other, or the volume of one or more separation chambers can be larger or smaller than that of other separation chambers. Preferably, they are evenly distributed among each other.

[0071] According to one embodiment of the present invention, the gas-liquid separation device also includes a gas-liquid separation component, which is respectively arranged inside the n separation chambers and is constructed to be able to perform the gas-liquid separation in the n separation chambers respectively to obtain corresponding n gas-phase materials and n liquid-phase materials.

[0072] According to one embodiment of the present invention, a washing device (preferably a washing aid distributor) or a cooling device (preferably a cooling aid distributor) is provided on the top and / or upper portion of the inner cavity.

[0073] According to one embodiment of the present invention, a stripping device (preferably a stripping aid distributor) is provided at the lower part and / or bottom of the inner cavity.

[0074] According to one embodiment of the present invention, the gas-liquid separation component is a gas-liquid enhanced contact device. According to the present invention, the gas-liquid enhanced contact device can be any type commonly known in the art, specifically, a column tray. According to the present invention, the column tray can be any type commonly known in the art, without particular limitation.

[0075] According to one embodiment of the present invention, the gas-liquid separation component is a centrifugal separator. According to the present invention, the centrifugal separator can be any type commonly known in the art, such as a cyclone separator. According to the present invention, the cyclone separator can be any type commonly known in the art, without particular limitation.

[0076] According to one embodiment of the present invention, the gas-liquid separation component is a filter. According to the present invention, the filter can be any type commonly known in the art, such as a demister. According to the present invention, the demister can be any type commonly known in the art, without particular limitation.

[0077] According to one embodiment of the present invention, the gas-liquid separation component is a stripping device. According to the present invention, the stripping device can be any type commonly known in the art, such as a stripping agent distributor. According to the present invention, the stripping agent distributor can be any type commonly known in the art, without particular limitation.

[0078] According to one embodiment of the present invention, the gas-liquid separation component is a washing device. According to the present invention, the washing device can be any type commonly known in the art, such as a detergent dispenser. According to the present invention, the detergent dispenser can be any type commonly known in the art, without particular limitation.

[0079] According to one embodiment of the present invention, the gas-liquid separation component is a cooling device. According to the present invention, the cooling device can be any type commonly known in the art, such as a cooling agent distributor. According to the present invention, the cooling agent distributor can be any type commonly known in the art, without particular limitation.

[0080] According to one embodiment of the present invention, the number of gas-liquid separation components provided in each separation chamber can be reasonably set according to actual needs, but as an example, can be independently selected from 0-20. In order to achieve a better technical effect of the present invention, it is preferred that the number of gas-liquid separation components provided in one or more separation chambers is different from that in other separation chambers, for example, the difference is 1-4 or 1-2.

[0081] According to one embodiment of the present invention, the cooling aid is selected from at least one of hydrocarbons such as light naphtha, naphtha, kerosene, light diesel, heavy diesel or hydrogenated tail oil, and can also be a partially condensed liquid phase (preferably light diesel, condensate) produced by cooling the gas phase. According to the present invention, there are no special restrictions on the operating parameters such as the temperature and flow rate of the cooling aid, and those skilled in the art can make reasonable choices based on actual conditions. In addition, the operating parameters of the cooling aid in different separation chambers can be the same or different from each other, but in order to achieve a better technical effect of the present invention, it is preferred that the operating parameters of the cooling aid in one or more separation chambers are different from those in other separation chambers, such as a difference of more than 5%.

[0082] According to one embodiment of the present invention, the washing aid is selected from at least one of hydrocarbons such as light naphtha, naphtha, kerosene, light diesel oil, heavy diesel oil or hydrogenated tail oil (preferably light diesel oil, condensate). According to the present invention, there is no particular restriction on the operating parameters such as the temperature and flow rate of the washing aid, and those skilled in the art can make reasonable choices based on actual conditions. In addition, the operating parameters of the washing aid in different separation chambers can be the same or different from each other, but in order to achieve a better technical effect of the present invention, it is preferred that the operating parameters of the washing aid in one or more separation chambers are different from those in other separation chambers, for example, the difference is more than 5%.

[0083] According to one embodiment of the present invention, the stripping aid is selected from gaseous hydrocarbons and / or water vapor; the water vapor can be steam such as low-pressure steam, dilution steam, medium-pressure steam and high-pressure steam; the gaseous hydrocarbon can be at least one of the vaporized gas phases of hydrocarbons such as light naphtha, naphtha, kerosene or light diesel (preferably water vapor) or a mixture thereof. According to the present invention, there is no special restriction on the operating parameters such as the temperature and flow rate of the stripping aid, and those skilled in the art can reasonably select them according to actual conditions. The temperature of the mixture is generally not higher than 550°C, preferably 300-500°C, and more preferably 350-450°C. In addition, the operating parameters of the stripping aid in different separation chambers can be the same or different from each other, but in order to achieve a better technical effect of the present invention, it is preferred that the operating parameters of the stripping aid in one or more separation chambers are different from those in other separation chambers, such as the difference is more than 5%.

[0084] According to one embodiment of the present invention, the gas-liquid separation feeding device is fluidly connected to the gas-liquid separation feed inlet, the cooling device is fluidly connected to the cooling aid inlet, the washing device is fluidly connected to the washing aid inlet, and the stripping device is fluidly connected to the stripping aid inlet.

[0085] According to one embodiment of the present invention, the outlet of the gas-liquid separation feed distributor, the washing aid distributor or the cooling aid distributor is toward the lower part of the inner cavity and the angle between the direction of the outlet and the central axis direction of the inner cavity is 0-90° (preferably 0°-30°).

[0086] According to one embodiment of the present invention, the outlet of the stripping aid distributor faces the upper part of the inner cavity, and the angle between the outlet and the central axis of the inner cavity is 0-90° (preferably 0-30°).

[0087] According to one embodiment of the present invention, the number of the gas-liquid separation feeding devices (preferably gas-liquid separation feeding distributors) provided in each of the separation chambers is independently selected from 1-5 (preferably 1-2).

[0088] According to one embodiment of the present invention, the number of the gas-liquid enhanced contact devices (preferably trays) provided in each of the separation chambers is independently selected from 0-20 (preferably 5-15).

[0089] According to one embodiment of the present invention, the number of the centrifugal separation devices (preferably cyclone separators) provided in each of the separation chambers is independently selected from 0-20 (preferably 5-15).

[0090] According to one embodiment of the present invention, the number of the filtering devices (preferably demisters) provided in each of the separation chambers is independently selected from 0-3 (preferably 1-2).

[0091] According to one embodiment of the present invention, the number of the stripping devices (preferably stripping aid distributors) provided in each of the separation chambers is independently selected from 0-3 (preferably 1-2).

[0092] According to one embodiment of the present invention, the number of the washing devices (preferably washing aid distributors) provided in each of the separation chambers is independently selected from 0-3 (preferably 1-2).

[0093] According to one embodiment of the present invention, the number of the cooling devices (preferably cooling aid distributors) provided in each of the separation chambers is independently selected from 0-3 (preferably 1-2).

[0094] According to one embodiment of the present invention, the gas-liquid separation component disposed within the mth separation chamber is different from the gas-liquid separation component disposed within the i-th separation chamber. Here, m and i are different and are each independently selected from integers from 1 to n. The inventors of the present invention have discovered that, particularly in the case of grouped or divided furnace feeding, when the feed composition varies, the number of gas-liquid separation components in the independent chambers can be flexibly set based on the properties of the group of raw materials, thereby further improving the gas-liquid separation effect of the group and ensuring that the group of raw materials is in the optimal steam cracking state.

[0095] According to this embodiment of the present invention, for example, the number of gas-liquid separation components provided in the mth separation chamber is different from the number of gas-liquid separation components provided in the ith separation chamber (preferably, the number difference is 1-4 or 1-2). Alternatively, for example, the type of gas-liquid separation component provided in the mth separation chamber is different from the type of gas-liquid separation component provided in the ith separation chamber.

[0096] According to this embodiment of the present invention, for more specific examples, 1) the gas-liquid separation component arranged inside the m-th separation chamber and the gas-liquid separation component arranged inside the ith separation chamber both include gas-liquid enhanced contact devices (preferably tower plates), but these devices differ in at least one indicator selected from the number of settings, separation efficiency, separation principle, operating parameters, device structure and size specifications; 2) the gas-liquid separation component arranged inside the m-th separation chamber and the gas-liquid separation component arranged inside the ith separation chamber both include centrifugal separation devices (preferably cyclone separators), but these devices differ in at least one indicator selected from the number of settings, separation efficiency, separation principle, device structure and size specifications; 3) the gas-liquid separation component arranged inside the m-th separation chamber and the gas-liquid separation component arranged inside the ith separation chamber both include filtering devices (preferably demisters), but these devices differ in at least one indicator selected from the number of settings, separation efficiency, separation principle, device structure and size specifications. , 4) the gas-liquid separation component arranged inside the m-th separation chamber and the gas-liquid separation component arranged inside the ith separation chamber both include a stripping device (preferably a stripping aid distributor), but these devices differ in at least one indicator selected from the number of settings, separation efficiency, separation principle, device structure and size specifications; 5) the gas-liquid separation component arranged inside the m-th separation chamber and the gas-liquid separation component arranged inside the ith separation chamber both include a washing device (preferably a washing aid distributor), but these devices differ in at least one indicator selected from the number of settings, separation efficiency, separation principle, device structure and size specifications; 6) the gas-liquid separation component arranged inside the m-th separation chamber and the gas-liquid separation component arranged inside the ith separation chamber both include a cooling device (preferably a cooling aid distributor), but these devices differ in at least one indicator selected from the number of settings, separation efficiency, separation principle, device structure and size specifications.

[0097] According to one embodiment of the present invention, a plurality of baffles are provided, and the angle between two adjacent baffles is 0-180° (preferably 30-90°).

[0098] According to one embodiment of the present invention, the baffle is longitudinally arranged inside the inner cavity along the central axis direction of the inner cavity, and the longitudinal edge of the baffle is sealed to the inner wall of the inner cavity, so that the n separation chambers form independent chambers.

[0099] According to one embodiment of the present invention, the upper edge of at least one (for example, all) of the baffles is sealedly connected to the side wall of the top of the inner cavity. Preferably, there is a gap (called a first gap) between the upper edge of at least one (for example, all) of the baffles and the side wall of the top of the inner cavity, thereby making the upper fluids of the n separation chambers connected to form a gas collecting chamber together with the top space of the inner cavity.

[0100] According to one embodiment of the present invention, there is a gap (called a second gap) between the lower edge of the baffle and the side wall of the bottom of the inner cavity, thereby connecting the lower fluids of the n separation chambers to form a liquid storage space together with the bottom space of the inner cavity.

[0101] According to one embodiment of the present invention, the cyclone separator is arranged at the upper part of the separation chamber, and the tower tray is arranged below the cyclone separator (for example, at the middle or lower part of the separation chamber).

[0102] According to one embodiment of the present invention, a collecting pipe is further provided in the gas-liquid separation device, wherein the liquid phase inlet of the collecting pipe is fluidically connected to the liquid phase outlet of the cyclone separator, and the liquid phase outlet of the collecting pipe is fluidically connected to the upper part of the tower plate.

[0103] According to one embodiment of the present invention, a sealing cover plate is horizontally arranged on the top of the inner cavity, and the periphery of the sealing cover plate is sealedly connected to the side wall of the inner cavity, so that the internal space of the inner cavity above the sealing cover plate forms a gas collecting chamber, and a plurality of openings are provided on the sealing cover plate, so that the internal space of the inner cavity below the sealing cover plate is fluidically connected to the gas collecting chamber via the plurality of openings.

[0104] According to one embodiment of the present invention, the upper edge of at least one (preferably all) of the baffles is sealed to the lower surface of the sealing cover plate, thereby arranging the n separation chambers in the inner space of the inner cavity below the sealing cover plate.

[0105] According to one embodiment of the present invention, the opening of the sealing cover plate is in fluid communication with the gas phase outlet of the cyclone separator, so that the gas phase separated by the cyclone separator can enter the gas collecting chamber.

[0106] According to one embodiment of the present invention, a downcomer is further provided in the gas-liquid separation device, wherein at least one of the openings of the sealing cover plate is fluidically connected to the downcomer, so that the liquid collected on the sealing cover plate is transported to the internal space below the sealing cover plate (preferably to the liquid storage space) via the downcomer.

[0107] According to one embodiment of the present invention, generally speaking, the height of the baffle (from top to bottom) is generally 4.5-11.5 m, but the present invention is sometimes not limited thereto.

[0108] According to certain embodiments of the present invention (hereinafter referred to as the first embodiment series), the cylindrical shell comprises, from top to bottom, a top head, a constant diameter cylinder, and a bottom head. Here, the constant diameter cylinder has an inner cavity diameter D of 3-10 m and an inner cavity height H of 5-12 m.

[0109] According to certain embodiments of the present invention (hereinafter referred to as the second embodiment series), the cylindrical shell includes, from top to bottom, a top head, a large-diameter cylinder, a first reduced diameter section, a small-diameter cylinder, a second reduced diameter section, and a bottom head. The inventors of the present invention have found that by providing a reduced diameter section, the liquid phase components separated in each cavity can be more easily gathered together under the guidance of the slope and discharged through the bottom liquid phase outlet, thereby further improving the separation effect of the gas-liquid separation device, further reducing the fluctuation range of the gasification rate, and ensuring that the group of raw materials is in the best steam cracking state. According to this embodiment of the present invention, the inner cavity diameter D1 of the large-diameter cylinder is 3-10m, and the inner cavity height H1 is 3-8m, and the inner cavity diameter D2 of the small-diameter cylinder is 1-5m, and the inner cavity height H2 is 1-4m. In addition, according to the present invention, it is preferred that the lower edge of the baffle extends to the small-diameter cylinder.

[0110] According to these embodiments of the present invention, preferably, the cyclone separator is disposed at the upper portion of the large-diameter cylinder, and the tower tray is disposed at the upper or middle portion of the small-diameter cylinder. The inventors of the present invention have discovered that after the gaseous and liquid phase components are initially separated by the cyclone separator, the liquid phase components entrained with the gaseous phase components in each cavity pass through the reduced diameter section to further increase the component concentration, and come into contact with the tower tray, further improving the heat transfer effect, thereby enhancing the separation effect of the gas-liquid separation device, and further reducing the fluctuation range of the gasification rate, ensuring that the group of feedstocks is in the optimal steam cracking state.

[0111] According to one embodiment of the present invention, the method for producing olefins by steam cracking further comprises step 3): combining at least two (e.g., all) of the n gaseous phase streams to form a comprehensive gaseous phase stream, and combining at least two (preferably all) of the n liquid phase streams to form a comprehensive liquid phase stream. According to the present invention, step 3) is an optional step, but is preferably a necessary step.

[0112] The inventors of the present invention have discovered that combining at least two (e.g., all) of the n gaseous materials to form a composite gaseous material offers significant advantages in finely adjusting the gasification rate compared to not combining the n gaseous materials at all. For example, cracking furnaces typically use average outlet temperature to control the heat load of the furnace. When at least two of the gaseous materials are combined to form a composite gaseous material, the high-temperature vapor-hydrocarbon mixture, after separation, is directly introduced into downstream equipment from the gaseous outlet of the separation chamber. This allows the fluctuation range of performance indicators such as the gasification rate of the separation chamber to be kept below 5%. Combined with the temperature control of the radiant section furnace tube outlet of the cracking furnace, this ensures that the feedstock group is in an optimal steam cracking state, thereby ensuring smooth operation of the cracking furnace, achieving optimal product yield and a long coke cleaning cycle, further reducing operating and maintenance costs and improving economic benefits.

[0113] In addition, by setting baffles to isolate the flash separation equipment into multiple separation chambers arranged side by side, there are also significant advantages in fine-tuning the vaporization rate compared to arranging multiple tanks in parallel and then combining the gas-phase outlet materials. Arranging multiple tanks makes it difficult to achieve uniform distribution of the vapor-hydrocarbon mixture in terms of floor space and piping space layout, resulting in a large fluctuation range in performance indicators such as the vaporization rate before the gas-phase materials are combined. After the gas-phase materials are combined, the fluctuation range of performance indicators such as the vaporization rate will also be significantly larger than when baffles are set to isolate the flash separation equipment into multiple separation chambers arranged side by side. In addition, setting baffles to isolate the flash separation equipment into multiple separation chambers arranged side by side also has significant advantages in reducing operating and maintenance costs and improving economic benefits.

[0114] According to one embodiment of the present invention, the method for producing olefins by steam cracking includes step 4): steam cracking at least one (preferably all) of the n gaseous materials, or the combined gaseous materials, to obtain a cracking product comprising the olefin. According to the present invention, the steam cracking can be carried out in any manner conventionally known in the art and is not particularly limited in the present invention.

[0115] According to one embodiment of the present invention, in step 4), at least one performance index of the gas phase material or the comprehensive gas phase material is monitored, and the operating parameters of at least one of the n separation chambers are maintained or changed according to the monitoring results. For example, the performance index is selected from at least one of the gas phase terminal boiling point, the liquid phase terminal boiling point, the gas phase heavy component content, the liquid phase light component content, and the gasification rate. In addition, for example, the operating parameter is selected from at least one of the gas-liquid mixture temperature, the gas-liquid mixture pressure, the gas-liquid mixture flow rate, the gas-liquid mixture distributor linear velocity, the cooling aid temperature, the cooling aid pressure, the cooling aid flow rate, the cooling aid distributor linear velocity, the washing aid temperature, the washing aid pressure, the washing aid flow rate, the washing aid distributor linear velocity, the stripping aid temperature, the stripping aid pressure, the stripping aid flow rate, and the stripping aid distributor linear velocity.

[0116] According to the present invention, the monitoring can be performed in any manner conventionally known in the art and is not particularly limited by the present invention. Taking a single-furnace cracking furnace as an example, during operation, the total feed hydrocarbon flow rate and the flow rates of each group of feed hydrocarbons are controlled, the cracking furnace outlet temperature is balanced and controlled, the steam-to-hydrocarbon ratio is controlled, and the furnace heat supply is controlled. The feed to each group of cracking furnace coils is controlled by a flow control valve. The flow rate is measured by a flow meter. These flow meters provide precise flow rates for each group of furnace tubes. A total feed rate controller adjusts the setpoints of each group of feed controllers to control the oil feed rate to each furnace. The steam-to-hydrocarbon ratio control controls the amount of dilution steam mixed with each group of feed. Monitoring the temperature of the gas-liquid mixture entering the flash separation device determines whether the operation meets the required performance index range. Furthermore, a thermocouple is installed at the outlet of each group of furnace tubes in the cracking furnace, and the average furnace outlet temperature is used to control the combustion load of each furnace. The furnace outlet temperature of each group of furnace tubes within the furnace is calculated to obtain the average furnace outlet temperature. When the cracking furnace's operating fluctuations intensify, the average furnace outlet temperature control will adjust the raw material feed flow rate to ensure stable device operation and keep the cracking reaction within the required range. In addition, with respect to performance indicators such as gasification rate, gas phase terminal boiling point, liquid phase terminal boiling point, gas phase heavy component content, and liquid phase light component content, the opening of the regulating valve on the pipeline is adjusted according to actual conditions to adjust the gas-liquid mixture pressure, gas-liquid mixture flow, or cooling agent pressure, cooling agent flow, and detergent pressure, detergent flow, etc., to ensure that the performance indicators are within the effective range. The fluctuation range of performance indicators such as the separation chamber gasification rate is controlled to below 5%. In combination with the control of the radiant section furnace tube outlet temperature of the above-mentioned cracking furnace, the raw materials are ensured to be in the optimal steam cracking state, thereby ensuring the stable operation of the cracking furnace, achieving the best product yield and a long coke cleaning cycle, further reducing operating and maintenance costs and improving economic benefits.

[0117] According to one embodiment of the present invention, it also relates to a gas-liquid separation method, comprising the step of transporting the gas-liquid separation feed through a gas-liquid separation feed device (preferably a gas-liquid separation feed distributor) into the gas-liquid separation device described in any one of the foregoing or subsequent aspects of the present invention to perform gas-liquid separation.

[0118] The present invention will be described in more detail below with reference to the accompanying drawings, but the present invention is not limited thereto.

[0119] First embodiment series

[0120] As shown in Figure 1, the gas-liquid separation device includes a vertical shell, a tower tray 7 arranged inside the vertical shell, a cyclone separator 6 arranged inside the vertical shell, a liquid storage space 10 and an optional baffle 9; the cyclone separator 6 is arranged at the upper part of the vertical shell, the tower tray 7 is arranged in the middle of the vertical shell and below the cyclone separator 6, and the liquid storage space 10 is arranged at the lower part or outside of the vertical shell; the baffle 9 is vertically arranged inside the vertical shell and the edge of the baffle 9 is sealed with the inner wall of the vertical shell to divide the upper space in the vertical shell into a plurality of separation chambers arranged side by side; the separation device includes a vapor-hydrocarbon mixture inlet 2, a cooling / washing aid inlet 4, a gas phase outlet 1, a liquid phase outlet 3 and an optional vapor The stripping aid inlet 5 of the separation device is used to communicate with the heavy hydrocarbon source so that the vapor hydrocarbon mixture can enter the separation device for gas-liquid separation; the cooling / washing aid inlet 4 of the separation device is used to communicate with the cooling aid source or the washing aid source so that the cooling aid or the washing aid can enter the separation device to cool or separate the vapor hydrocarbon mixture; the stripping aid inlet 5 of the separation device is used to communicate with the stripping aid source so that the stripping aid can enter the separation device for stripping treatment; the gas phase outlet 1 of the separation device is used to communicate with the gas phase downstream device so that the separated gas phase components can enter the gas phase downstream device; the liquid phase outlet 3 of the separation device is used to communicate with the liquid phase downstream device so that the separated liquid phase components can enter the liquid phase downstream device for further use.

[0121] According to one embodiment of the present invention, by injecting a cooling aid, a washing aid, and an optional stripping aid, the content of heavy fractions and impurities such as colloids in the gas phase can be reduced, thereby improving the gas-liquid separation effect and preventing coking in the radiant section, thereby extending the decoking cycle of the cracking furnace; and the content of light components in the liquid phase can be reduced. Injecting a washing aid or a stripping aid can maximize the stripping of light components from the liquid phase to maximize the yield of light components; injecting a cooling aid can control the vaporization rate and reduce heavy component entrainment, while increasing the liquid phase flow rate to improve the separation effect of the trays. Furthermore, the present invention uses baffles to isolate the flash separation equipment into multiple, side-by-side separation chambers. Each separation chamber is equipped with a feed inlet and a gas phase outlet. After separation, the high-temperature gas-hydrocarbon mixture entering the separation chamber directly enters the downstream device through the gas phase outlet of the separation chamber, eliminating the need to adjust the hydrocarbon partial pressure by installing a high-temperature regulating valve on the gas phase outlet pipeline. This can reduce the failure rate of the high-temperature regulating valve at high temperatures and thus extend the life of the system. In addition, the installation of a cyclone separator and a tray in each separation chamber can improve the gas-liquid separation efficiency and the flash evaporation effect to further reduce the entrainment of impurities such as heavy components and colloids, avoid their coking in the radiation section, and further extend the decoking cycle of the cracking furnace.

[0122] According to one embodiment of the present invention, the cooling aid, washing aid and stripping aid can be liquid hydrocarbons and / or water vapor; the water vapor can be steam such as low-pressure steam, medium-pressure steam and high-pressure steam; the liquid hydrocarbons can be hydrocarbons such as light naphtha, naphtha, kerosene, light diesel, heavy diesel or hydrogenated tail oil.

[0123] According to one embodiment of the present invention, the vertical shell is a conventional choice in the art, and the present invention can reasonably select according to different needs. For example, the vertical shell can be a cylinder with equal diameters sealed at the top and bottom, or a cylinder including a first diameter, a reduced diameter section, and a second diameter connected in sequence from top to bottom, wherein the first diameter is larger than the second diameter.

[0124] According to one embodiment of the present invention, the gas phase outlet 1 is arranged at the top of the vertical shell for communicating with the gas phase downstream device so that the gas phase components separated by the separation device can enter the gas phase downstream device for use. The liquid phase outlet 3 is arranged at the bottom of the vertical shell for communicating with the liquid phase downstream device so that the liquid phase components obtained by the separation device can enter the liquid phase downstream device for use. The vapor-hydrocarbon mixture inlet 2, the cooling / washing aid inlet 4 and the optional stripping aid inlet 5 are arranged on the side of the above-mentioned vertical shell. The vapor-hydrocarbon mixture inlet 2 is used to communicate with the heavy hydrocarbon source so that the mixed raw material can enter the separation device; the cooling / washing aid inlet 4 is used to communicate with the cooling aid source or the washing aid source so that the cooling aid or the washing aid can enter the separation device to participate in the separation process; the stripping aid inlet 5 is used to communicate with the stripping aid source so that the stripping aid can enter the separation device to participate in the separation process.

[0125] According to one embodiment of the present invention, the vapor-hydrocarbon mixture inlet 2 of the gas-liquid separation device can be arranged on the same horizontal line as the cooling / washing aid inlet 4. In this case, the separation device is provided with a stripping aid inlet 5 and the stripping aid inlet 5 is arranged below the vapor-hydrocarbon mixture inlet 2; the vapor-hydrocarbon mixture inlet 2 of the separation device can also be arranged below the cooling / washing aid inlet 4. In this case, the separation device is not provided with a stripping aid inlet 5.

[0126] According to one embodiment of the present invention, it further includes a raw material pipeline a, a cooling / washing aid pipeline c and an optional stripping aid pipeline d; the inlet of the raw material pipeline a is connected to the heavy hydrocarbon source, and the outlet is connected to the vapor-hydrocarbon mixture inlet 2 of the vertical shell, so that the vapor-hydrocarbon mixture raw material can enter the separation device through the raw material pipeline a; the inlet of the cooling / washing aid pipeline c is connected to the cooling aid source or the washing aid source, and the outlet is connected to the cooling / washing aid inlet 4 of the vertical shell, so that the cooling aid or the washing aid can enter the separation device through the cooling / washing aid pipeline c; the inlet of the stripping aid pipeline d is connected to the stripping aid source, and the outlet is connected to the stripping aid inlet 5 of the vertical shell, so that the stripping aid can enter the separation device through the stripping aid pipeline d; the raw material pipeline a is provided with a feed preheater for heating the material in the raw material pipeline a. In addition, a raw material branch line is set in parallel on the raw material pipeline a, and the connection points of the raw material main line of the raw material branch line are on the left and right sides of the feed preheater. Through the setting of the raw material branch line, the temperature of the raw material entering the separation device can be flexibly adjusted.

[0127] According to one embodiment of the present invention, it further includes a steam pipeline b; the raw material pipeline a is provided with a primary steam inlet and a secondary steam inlet; the stripping agent pipeline d is provided with a secondary steam inlet; the steam pipeline b can be divided into a primary steam pipeline b1 and a secondary steam pipeline b2; the inlets of the primary steam pipeline b1 and the secondary steam pipeline b2 are used to communicate with a steam source, so that the steam can be divided into primary steam and secondary steam through the steam pipeline b; the outlet of the primary steam pipeline b1 is communicated with the primary steam inlet on the raw material pipeline a, so that the primary steam can enter the raw material pipeline a and mix with the raw material, and the outlet of the secondary steam pipeline b2 is communicated with the secondary steam inlets on the raw material pipeline a and the stripping agent pipeline d, so that the secondary steam can enter the raw material pipeline a and the stripping agent pipeline d respectively; the primary steam pipeline b1 and the secondary steam pipeline b2 are provided with steam preheaters for heating the steam. In addition, steam branches are provided on the primary steam pipeline b1 and the secondary steam pipeline b2, and the connection points of the steam branches with the primary steam pipeline and the secondary steam pipeline are on the left and right sides of the steam preheater, which can flexibly adjust the steam temperature.

[0128] According to one embodiment of the present invention, the feed preheater and the dilution steam preheater are independently selected from one or more of a heating furnace, a cracking furnace convection section and a heat exchanger.

[0129] According to one embodiment of the present invention, the steam entering the steam line b includes one of dilution steam, low-pressure steam, medium-pressure steam or high-pressure steam.

[0130] According to one embodiment of the present invention, by adjusting the flow rate of the heating medium or the heater power in the feed preheater and the steam preheater, the temperature of the feed preheater and the primary steam and secondary steam preheaters can be flexibly controlled, thereby flexibly controlling the phase and temperature of the vapor-hydrocarbon mixture delivered to the gas-liquid separation device, and further flexibly controlling the separation effect of the flash separation.

[0131] According to one embodiment of the present invention, one or more baffles 9 are disposed within the vertical housing to divide the interior of the vertical housing into a plurality of side-by-side separation chambers. The angle between two adjacent baffles 9 is 0-180°, preferably 60-120°, and more preferably 90°. For example, in a specific embodiment of the present invention, as shown in FIG3 , the gas-liquid separation device comprises four baffles 9 , with the angle between two adjacent baffles 9 being 90°, thereby dividing the interior space of the vertical housing into four separation chambers of equal size.

[0132] According to one embodiment of the present invention, a gas phase outlet 1 is provided at the top of the separation chamber for communicating with a gas phase downstream device so that the gas phase separated by the separation chamber can enter a subsequent gas phase downstream device.

[0133] According to one embodiment of the present invention, a liquid phase outlet 3 is provided at the bottom of the separation chamber for communicating with a liquid phase downstream device so that the liquid phase components separated by each separation chamber can enter a subsequent liquid phase downstream device.

[0134] According to one embodiment of the present invention, a vapor-hydrocarbon mixture inlet 2, a cooling / washing aid inlet 4 and an optional stripping aid inlet 5 are further provided on the side wall of the separation chamber; the vapor-hydrocarbon mixture inlet 2 of the separation chamber is used to communicate with a heavy hydrocarbon source; the cooling / washing aid inlet 4 of the separation chamber is used to communicate with a cooling aid source or a washing aid source; the stripping aid inlet 5 of the separation chamber is used to communicate with a stripping aid source; so that the vapor-hydrocarbon mixture, the cooling aid and the stripping aid can enter the separation device through the vapor-hydrocarbon mixture inlet 2, the cooling / washing aid inlet 4 and the stripping aid inlet 5 respectively to participate in the separation treatment.

[0135] According to one embodiment of the present invention, in order to further enhance the gas-liquid separation effect, the relative positions of the vapor-hydrocarbon mixture inlet 2, the cooling / washing aid inlet 4, and the optional stripping aid inlet 5 are reasonably arranged. For example, the positional relationship between the various inlets can be such that the vapor-hydrocarbon mixture inlet 2 and the cooling / washing aid inlet 4 are on the same horizontal line, with the stripping aid inlet 5 positioned below; alternatively, the cooling / washing aid inlet 4, the vapor-hydrocarbon mixture inlet 2, and the stripping aid inlet 5 are positioned sequentially from top to bottom; or alternatively, the cooling / washing aid inlet 4 and the vapor-hydrocarbon mixture inlet 2 are positioned sequentially from top to bottom. Whether the stripping aid inlet and the cooling / washing aid inlet 4 are provided to inject cooling aid or washing aid, as well as the positional relationship between the various inlets, should be determined based on the properties of the heavy hydrocarbon feedstock and operating procedures.

[0136] According to one embodiment of the present invention, when the vapor-hydrocarbon mixture inlet 2 and the cooling / washing aid inlet 4 are at the same horizontal line, the feeding device connected to the vapor-hydrocarbon mixture inlet 2 and the feeding device connected to the cooling / washing aid inlet 4 can be connected through a linking assembly. The linking assembly is conventionally selected in the art so that the materials entering through the vapor-hydrocarbon mixture inlet 2 and the cooling / washing aid inlet 4 can be evenly mixed in the linking assembly.

[0137] According to one embodiment of the present invention, the cooling / washing aid inlet 4 and the vapor-hydrocarbon mixture inlet 2 are both disposed below the inlet of the cyclone separator 6. In this embodiment, the problem of the vapor-hydrocarbon mixture, cooling aid, and washing aid entering the cyclone separator 6 and affecting the gas-liquid separation effect can be avoided.

[0138] According to one embodiment of the present invention, as shown in Figure 1, when the vapor-hydrocarbon mixture inlet 2 and the cooling / washing aid inlet 4 are on the same horizontal line, they are both arranged below the inlet of the cyclone separator 6; the stripping aid inlet 5 is arranged below and between the liquid storage space 10 and the tower tray 7, and the separation chamber also includes a feed and cooling aid mixing distributor and a stripping aid distributor.

[0139] According to one embodiment of the present invention, the two inlets of the feed and cooling aid mixing distributor extend to the outside of the separation chamber respectively to form the vapor-hydrocarbon mixture inlet 2 and the cooling / washing aid inlet 4; the outlet of the feed and cooling aid mixing distributor is arranged toward the lower part of the vertical shell and the angle α between the direction of the outlet and the axial direction of the vertical shell is 0-90°.

[0140] According to one embodiment of the present invention, the inlet of the stripping agent distributor extends to the outside of the separation chamber to form the stripping agent inlet 5; the outlet of the stripping agent distributor is arranged toward the upper part of the vertical shell and the angle β between the direction of the outlet and the axial direction of the vertical shell is 0-90°.

[0141] According to one embodiment of the present invention, a vapor-hydrocarbon mixture and a cooling agent are introduced into a feed and cooling agent mixing distributor through both ends thereof and mixed, thereby causing the vapor-hydrocarbon mixture to undergo preliminary condensation. The preliminary condensed material then enters a separation chamber through the distributor outlet. The stripping agent is sprayed upward through the stripping medium distributor, allowing it to fully contact the preliminary condensed material above, further enhancing the stripping effect and, in turn, the gas-liquid separation effect and efficiency.

[0142] According to one embodiment of the present invention, as shown in FIG2 , when the cooling / washing aid inlet 4 and the vapor-hydrocarbon mixture inlet 2 are arranged sequentially from top to bottom, the separation chamber further includes a feed distributor and a washing aid distributor.

[0143] According to one embodiment of the present invention, the inlet of the feed distributor extends to the outside of the separation chamber to form the vapor-hydrocarbon mixture inlet 2; the outlet of the feed distributor is arranged toward the upper part of the vertical shell and the angle η between the direction of the outlet and the axial direction of the vertical shell is 0-90°.

[0144] According to one embodiment of the present invention, the inlet of the washing aid distributor extends to the outside of the separation chamber to form the cooling / washing aid inlet 4; the outlet of the washing aid distributor is arranged toward the lower part of the vertical shell and the angle γ between the direction of the outlet and the axial direction of the vertical shell is 0-90°.

[0145] According to one embodiment of the present invention, the feed distributor can be used to spray the vapor-hydrocarbon mixture upward so that the gas phase in the vapor-hydrocarbon mixture can flow from bottom to top and the liquid phase can flow from top to bottom, further enhancing the separation effect and separation efficiency. The detergent distributor can be used to make the detergent flow downward, thereby making the detergent fully contact with the vapor-hydrocarbon mixture, effectively preventing the entrainment of heavy fractions and impurities in the gas phase components, and avoiding the phenomenon of coking when entering the downstream device; wherein, the heavy fractions and impurities include one or more of colloids, asphaltenes, metal impurities, sulfur, oxygen, nitrogen and heavy components. In addition, the heights of the feed distributors, cooling agent distributors and stripping agent distributors in the multiple separation chambers can be the same or different, depending on the temperature and pressure of the vapor-hydrocarbon mixture.

[0146] According to one embodiment of the present invention, the feed distributor, feed and cooling aid mixing distributor, washing aid distributor and stripping aid distributor are provided with multiple open areas as outlets of the distributor; the porosity of the open areas is 5-15%, and the average pore diameter of the openings in the open areas is 10-20 mm.

[0147] According to one embodiment of the present invention, the cooling / washing aid inlet comprises a liquid hydrocarbon inlet and / or a water inlet; the stripping aid inlet comprises a liquid hydrocarbon inlet and / or a water inlet.

[0148] According to one embodiment of the present invention, the separation chamber includes a cyclone separator 6, a tower tray 7 and a liquid storage space 10 arranged in sequence from top to bottom.

[0149] According to one embodiment of the present invention, as shown in Figure 1, the cyclone separator 6 is arranged in the upper space of the separation chamber, so that the vapor-hydrocarbon mixture entering the separation chamber can be separated into a gas phase component and a liquid phase component through the cyclone separator 6; the tower tray 7 is arranged in the middle of the separation chamber and is located below the cyclone separator 6, so that the liquid phase component separated by the cyclone separator 6 in the separation chamber can be further separated through the tower tray 7; the liquid storage space 10 is arranged in the lower space of the separation chamber, so that the liquid phase component further separated by the tower tray 7 in the separation chamber can flow into the liquid storage space 10.

[0150] According to one embodiment of the present invention, the liquid storage space 10 can be independently provided outside the separation chamber.

[0151] According to one embodiment of the present invention, the tower tray 7 and the cyclone separator 6 are conventionally selected in the art, and the present invention does not make any special requirements.

[0152] According to one embodiment of the present invention, a collecting pipe is further provided in the separation chamber; the collecting pipe includes a liquid phase inlet and a liquid phase outlet 3, the liquid phase inlet of the collecting pipe is connected to the liquid phase outlet 3 of the cyclone separator 6, and the liquid phase outlet 3 of the collecting pipe extends to the inlet of the tower tray 7.

[0153] According to one embodiment of the present invention, the vapor-hydrocarbon mixture first enters the cyclone separator 6 for preliminary separation, the separated gas phase component is discharged through the gas phase outlet 1 of the cyclone separator 6, the separated liquid phase component passes through the outlet at the bottom of the material leg of the cyclone separator 6 and enters the tower plate 7 below through the collecting pipe, and is further separated through the tower plate 7 to obtain the final liquid phase component, and the obtained liquid phase component enters the liquid storage space 10 at the bottom of the separation chamber through the outlet of the tower plate 7.

[0154] According to one embodiment of the present invention, the number of stages of the cyclone separators 6 inside the separation chamber is one or more; when the number of stages of the cyclone separators 6 inside each of the separation chambers is one, the lower end outlet of the cyclone separators 6 is connected to the inlet of the manifold, so that the liquid separated by the above-mentioned cyclone separators can enter the liquid collection area below through the manifold. If the number of stages of the cyclone separators 6 inside each of the separation chambers is , there is a gap between the outer walls of the material legs of the multiple cyclone separators 6, and the lengths of the material legs of the multiple cyclone separators 6 are successively longer from the outside to the inside; the lower end outlets of the multiple cyclone separators 6 are all connected to the inlet of the manifold, so that all the liquid separated by the above-mentioned multiple cyclone separators can enter the tower tray 7 below through the manifold.

[0155] According to one embodiment of the present invention, a cooling / washing aid storage or distributor is provided below the inlet of the upper cyclone separator of the separation chamber, so that the gas phase components obtained by flash separation in the separation chamber can be cooled or the heavy components entrained in the gas phase can be condensed into large liquid particles or condensed or absorbed by the washing aid and enter the tower tray below for further separation.

[0156] According to one embodiment of the present invention, a sealing cover plate 8 is further provided in each separation chamber. The sealing cover plate 8 is horizontally arranged above the cyclone separator 6, and the edge of the sealing cover plate 8 is tightly coupled to the sidewall of the separation chamber, so that the space above the sealing cover plate 8 forms a gas collection chamber. The sealing cover plate 8 is provided with a gas phase opening, and the gas phase opening is connected to the gas phase outlet 1 of the cyclone separator 6, so that the gas phase separated by the cyclone separator 6 can enter the gas collection chamber. In this embodiment, the provision of the sealing cover plate 8 allows the gas phase components in the separation chamber to be discharged from the separation device only through the gas phase outlet 1 of the cyclone separator 6, further improving the gas-liquid separation effect.

[0157] According to one embodiment of the present invention, as shown in FIG1 , a method for treating heavy hydrocarbons using the system of the present invention includes:

[0158] A heavy hydrocarbon feedstock is mixed with primary dilution steam heated in a dilution steam preheater after passing through a feed preheater to form a vapor-hydrocarbon mixture at a temperature of 100-400°C (preferably 200-370°C); the vapor-hydrocarbon mixture enters a feed and cooling aid mixing distributor through vapor-hydrocarbon mixture inlet 2 of a gas-liquid separation device; a cooling aid enters the other end of the feed and cooling aid mixing distributor through a cooling / washing aid pipeline c; the vapor-hydrocarbon mixture and the cooling aid contact in the feed and cooling aid mixing distributor before entering a separation device; wherein the angle α between the outlet of the feed and cooling aid mixing distributor and the axial direction of the shell is 0-90°; and the cooling aid is selected from liquid hydrocarbons and / or water.

[0159] According to one embodiment of the present invention, the stripping aid enters the stripping aid inlet 5 of the separation device through the stripping aid pipeline d and then enters the gas-liquid separation device through the stripping aid distributor; wherein the angle β between the direction of the gas outlet and the axial direction is 0-90°; the stripping aid is selected from liquid hydrocarbons and / or water.

[0160] According to one embodiment of the present invention, a mixture of a vapor hydrocarbon mixture and a cooling aid is brought into countercurrent contact with a stripping aid, and the gaseous material enters a cyclone separator 6 for preliminary separation treatment, so that the gaseous component enters the gas collecting chamber from the gas phase outlet of the cyclone separator 6; the obtained liquid phase component enters the tower tray 7 from the liquid phase outlet 3 of the cyclone separator 6 and the collecting pipe, is further processed through the tower tray 7, and the obtained liquid phase component is sent to the liquid storage space 10 below; the gaseous phase product in the gas collecting chamber is discharged through the gas phase outlet 1, and the liquid phase product in the liquid storage space 10 is discharged through the liquid phase outlet 3.

[0161] Second embodiment series

[0162] According to one embodiment of the present invention, as shown in Figure 5, the gas-liquid separation device includes at least a vertical shell 1, a cyclone separator group 5 arranged inside the vertical shell 1, a tower tray 3 arranged inside the vertical shell 1, a liquid collection area 9 and an optional baffle 10.

[0163] According to one embodiment of the present invention, the cyclone separator group 5 is arranged on the upper part of the vertical shell 1; the tower tray 3 is arranged below the cyclone separator group 5; and the liquid collection area 9 is arranged below the tower tray 3.

[0164] According to one embodiment of the present invention, the baffle 10 is vertically arranged inside the vertical shell 1, and the upper edge of the baffle 10 is sealedly connected to the top of the vertical shell 1, so as to divide the upper space inside the vertical shell 1 into a plurality of separation chambers arranged side by side; a gap is formed between the lower edge of the baffle 10 and the bottom of the vertical shell 1, so as to form the liquid collection area 9 in the lower space inside the vertical shell 1, and each of the separation chambers is respectively connected to the liquid collection area 9, and a liquid phase outlet 16 is provided at the bottom of the liquid collection area 9;

[0165] According to one embodiment of the present invention, a flow diversion distribution module 2 and an inlet steam distributor 4 are further provided inside the vertical shell 1; the flow diversion distribution module 2 includes a first flow diversion distribution module and a second flow diversion distribution module; the inlet of the inlet steam distributor 4 extends to the outside of the vertical shell 1 to form a cooling / washing aid inlet 13; the inlet of the first flow diversion distribution module extends to the outside of the vertical shell 1 to form a steam-hydrocarbon mixture inlet 12; the inlet of the second flow diversion distribution module extends to the outside of the vertical shell 1 to form a stripping aid inlet 14.

[0166] According to the present invention, the reaction materials entering the gas-liquid separation device are evenly distributed by using an inlet steam distributor 4, a first flow guide distribution module, and a second flow guide distribution module, which can effectively avoid the problem of poor flash evaporation and deliquescence due to uneven feed concentration. In addition, by using a cyclone separator group 5, the shear stress of the cyclone field and the sedimentation effect of the spatial gravity field of the cyclone separator can be utilized to enhance the separation effect of steam removal of crude oil droplets, reduce the separation time, and avoid the problem of flash evaporation of gas phase entrained droplets. Optionally, the vertical shell 1 is isolated into multiple separation chambers arranged side by side by a baffle 10. After separation, the high-temperature raw materials entering the separation chamber directly enter the downstream device from the gas phase outlet of the above-mentioned separation chamber. There is no need to set a high-temperature regulating valve, which can reduce the failure rate of the high-temperature regulating valve at high temperatures, and thus can improve the life of the system.

[0167] According to one embodiment of the present invention, the vertical shell 1 is a conventional choice in the field and can be reasonably selected according to different needs. For example, the vertical shell 1 is a cylindrical shell; the cylindrical shell can be a cylinder with equal diameters sealed at the top and bottom, or it can include a large-diameter cylinder, a first reduced-diameter section, a small-diameter cylinder, and a second reduced-diameter section from top to bottom.

[0168] According to one embodiment of the present invention, the lower edge of the baffle 10 extends to the lower portion of the small-diameter cylinder.

[0169] According to one embodiment of the present invention, the second necking section and a portion of the lower portion of the small-diameter cylinder form a liquid collection area 9 .

[0170] According to one embodiment of the present invention, the cyclone separator group 5 is arranged on the upper part of the large-diameter cylinder.

[0171] According to one embodiment of the present invention, the tower tray 3 is arranged on the upper part of the small-diameter cylinder.

[0172] According to one embodiment of the present invention, the liquid phase outlet 16 is arranged at the bottom of the vertical shell 1, and the gas phase outlet 15 is arranged at the top of the vertical shell 1, so that the separated gas phase material can enter the subsequent processing device through the gas phase outlet 15 at the top, and the liquid phase material can enter the subsequent processing device.

[0173] According to one embodiment of the present invention, the cooling / washing aid inlet 13 and the vapor-hydrocarbon mixture inlet 12 are both disposed on the sidewall of the large-diameter cylindrical portion of the vertical housing; the stripping aid inlet 14 is disposed on the sidewall of the small-diameter cylindrical portion of the vertical housing. Furthermore, the positional relationship between the cooling / washing aid inlet 13 and the vapor-hydrocarbon mixture inlet 12 needs to be determined based on actual operational requirements. For example, the cooling / washing aid inlet 13 and the vapor-hydrocarbon mixture inlet 12 may be co-located or positioned below the vapor-hydrocarbon mixture inlet 12.

[0174] According to one embodiment of the present invention, when the cooling / washing aid inlet 13 is below the vapor-hydrocarbon mixture inlet 12, the inlet steam distributor 4 is arranged above the first diversion distribution module, with some distance between the two. When the cooling / washing aid inlet 13 and the vapor-hydrocarbon mixture inlet 12 can be on the same horizontal line, the inlet steam distributor 4 and the first diversion distribution module are also arranged on the same horizontal line, and the inlet steam distributor 4 and the first diversion distribution module are connected via a linking component. The linking component is conventionally selected in the art so that the materials entering through the vapor-hydrocarbon mixture inlet 12 and the cooling / washing aid inlet 13 can be evenly mixed in the linking component.

[0175] According to one embodiment of the present invention, the cooling / washing aid inlet 13 of the gas-liquid separation device is connected to a cooling / washing aid source via a pipeline; the vapor-hydrocarbon mixture inlet 12 is connected to a vapor-hydrocarbon mixture source via a pipeline; and the stripping aid inlet 14 is connected to a stripping aid source via a pipeline. In this embodiment, the cooling aid and washing aid used in the cooling / washing aid source, and the stripping aid used in the stripping aid source, can each be independently selected from liquid hydrocarbons and / or water vapor; the water vapor can be low-pressure steam, medium-pressure steam, or high-pressure steam; and the liquid hydrocarbon can be light naphtha, naphtha, kerosene, light diesel oil, heavy diesel oil, or hydroprocessing tail oil, among other hydrocarbons.

[0176] According to one embodiment of the present invention, the baffles 10 can be selected from conventional ones in the art and are not particularly required by the present invention. The number of adjacent baffles 10 can be 0, 1, 2, 3, 4, or more than 4, preferably less than 4.

[0177] According to one embodiment of the present invention, when the number of baffles 10 is 2, the angle between two adjacent baffles 10 can be 180°; when the number of baffles 10 is 3, the angle between two adjacent baffles 10 can be 120°; when the number of baffles 10 is 4, the angle between two adjacent baffles 10 can be 90°.

[0178] According to one embodiment of the present invention, the cyclone separator group 5 is mainly composed of one or more cyclones. Preferably, the number of cyclones in the cyclone separator group 5 is 2 or more, more preferably 6. N cyclones are connected in series to form an n-stage cyclone separator group. For example, a three-stage cyclone separator is formed by three cyclones connected in series.

[0179] According to one embodiment of the present invention, the cyclone separator group 5 is composed of two groups of three-stage cyclone separators.

[0180] According to one embodiment of the present invention, the inlet of the three-stage cyclone separator is located at the upper part of the large diameter cylinder, and the end of the feed leg of the three-stage cyclone separator extends to the lower part of the large diameter cylinder or the first necking section.

[0181] According to one embodiment of the present invention, the three-stage cyclone separator is composed of a first-stage cyclone separator, a second-stage cyclone separator and a third-stage cyclone separator connected in series, and the first-stage cyclone separator is located inside the separation chamber, and the third-stage cyclone separator is located outside the separation chamber; specifically, the gas phase outlet of the first-stage cyclone separator is connected to the gas phase inlet of the second-stage cyclone separator, and the gas phase outlet of the second-stage cyclone separator is connected to the gas phase inlet of the third-stage cyclone separator.

[0182] According to one embodiment of the present invention, the lengths of the feed legs of the three-stage cyclone separators may be the same or different. Preferably, the length of the feed leg of the first-stage cyclone separator is greater than the length of the feed leg of the second-stage cyclone separator, and the length of the feed leg of the second-stage cyclone separator is greater than the length of the feed leg of the third-stage cyclone separator.

[0183] According to one embodiment of the present invention, a horizontal partition plate 7 is further provided in the separation chamber; the horizontal partition plate 7 is arranged horizontally above the cyclone separator group 5 and the edge of the horizontal partition plate 7 is tightly combined with the side wall of the separation chamber so that the upper space of the horizontal partition plate 7 forms an overflow collection chamber 8.

[0184] According to one embodiment of the present invention, a gas phase opening is provided on the horizontal partition plate 7 and the gas phase opening is connected to the gas phase outlet of the cyclone separator group 5, so that the gas phase separated by the cyclone separator group 5 can enter the overflow collection chamber 8.

[0185] According to one embodiment of the present invention, a downcomer group 6 is provided in the separation chamber; a downcomer opening is provided on the horizontal partition plate 7; the inlet of the downcomer group 6 is connected to the downcomer opening on the horizontal partition plate 7, and the outlet of the downcomer group 6 extends downward to above the liquid collecting area 9, so that the liquid phase in the overflow collecting chamber 8 can enter the liquid collecting area 9 through the downcomer group 6.

[0186] According to one embodiment of the present invention, a manifold 11 is further provided in the separation chamber, and the manifold 11 includes a liquid phase inlet and a liquid phase outlet; the liquid phase inlet of the manifold 11 is connected to the liquid phase outlet of the cyclone separator group 5, and the liquid phase outlet of the manifold 11 extends downward to above the liquid collection area 9, so that the liquid phase separated by the cyclone separator group 5 can enter the liquid collection area 9 through the manifold 11.

[0187] According to one embodiment of the present invention, the shape of the manifold 11 can be one or more of a I-shaped tube, a V-shaped tube, and an L-shaped tube, preferably a V-shaped tube.

[0188] According to one embodiment of the present invention, the included angle of the V-shaped tubular body may be consistent with the included angle between the necking section and the small diameter cylinder.

[0189] According to one embodiment of the present invention, a fixing piece is further provided in the separation chamber for fixing the manifold 11 inside the vertical housing 1 .

[0190] According to one embodiment of the present invention, the tower tray 3 is conventionally selected in the art and is not particularly required by the present invention.

[0191] According to one embodiment of the present invention, the lower surface of the inlet steam distributor 4, the lower surface of the first diversion distribution module and the upper surface of the second diversion distribution module in the separation chamber are all provided with multiple opening areas as material nozzles; the porosity of the opening areas is 5-15%, and the average pore diameter of the openings in the opening areas is 10-20 mm.

[0192] According to one embodiment of the present invention, the angle α between the direction of the material nozzle of the inlet steam distributor 4 and the axial direction of the vertical shell 1 is 0-90°.

[0193] According to one embodiment of the present invention, a material nozzle is provided on the lower surface of the first flow diversion distribution module; an angle β between the direction of the material nozzle of the first flow diversion distribution module and the axial direction of the vertical shell 1 is 0-90°.

[0194] According to one embodiment of the present invention, an angle γ between the direction of the material nozzle of the second flow distribution module and the axial direction of the vertical shell 1 is 0-90°.

[0195] According to one embodiment of the present invention, the first flow diversion and distribution module is arranged below the inlet of the cyclone separator group 5 ; the second flow diversion and distribution module is arranged below the inlet of the tower tray 3 .

[0196] According to one embodiment of the present invention, a gas phase outlet 15 is provided at the top of the separation chamber, so that the gas phase separated by the gas-liquid separation device is discharged from the device through the gas phase outlet 15 .

[0197] According to one embodiment of the present invention, the steam-hydrocarbon mixture is uniformly mixed in the separation chamber through the first diversion distribution module, the washing aid or cooling medium is uniformly mixed through the inlet steam distributor 4, and the stripping aid is uniformly mixed through the second diversion distribution module, thereby enhancing the stripping effect and further enhancing the gas-liquid separation effect and separation efficiency.

[0198] According to one embodiment of the present invention, as shown in FIG5 , the method for producing olefins by steam cracking of the present invention comprises: passing a heavy hydrocarbon feedstock heated to 100-400° C. (preferably 200-370° C.) through a first diversion distribution module into a separation chamber; passing a cooling agent through an inlet steam distributor 4 into the separation chamber; passing a stripping agent through a second diversion distribution module into the separation chamber; allowing a mixture of a steam-hydrocarbon mixture and a cooling agent to contact the stripping agent in countercurrent, and the gaseous material enters a cyclone separator group 5 for preliminary separation. The separation treatment is carried out so that the gas phase components enter the overflow collection chamber 8 from the gas phase outlet of the cyclone separator group 5, and the liquid phase in the overflow collection chamber 8 enters the liquid collection area 9 through the downcomer group 6; the obtained liquid phase components enter the manifold 11 from the material legs of the cyclone separator group 5, and enter the tower plate 3 through the outlet of the manifold 11, and then enter the liquid collection area 9 after further separation through the tower plate 3; the gas phase product in the overflow collection chamber 8 is discharged through the gas phase outlet 15, and the liquid phase product in the liquid collection area 9 is discharged through the liquid phase outlet 16.

[0199] Example

[0200] The present invention is further described in detail below using examples and comparative examples, but the present invention is not limited to these examples.

[0201] The raw materials used in the examples and comparative examples were all obtained from commercial sources.

[0202] The control index in the embodiment and the comparative example is the gasification rate at the gas phase outlet, the final distillation point is controlled to be approximately 445° C., and the control index value acquisition time is 6 hours.

[0203] Example 1

[0204] A heavy hydrocarbon feedstock with an API value of 40 is used. As shown in Figure 1, the gas-liquid separation device comprises four baffles 9, with adjacent baffles 9 forming a 90° angle between each other, dividing the interior of the vertical shell into four equally sized separation chambers. The operating temperature of each chamber is maintained at 280°C and the operating pressure at 0.4 MPaG by thermometers and regulating valves installed in front of each chamber. The stripping agent is steam, and the cooling agent is diesel. From top to bottom, the vertical shell comprises a top head, a cylinder of uniform diameter, and a bottom head. D = 5 m, H = 8 m. The baffle height is 7 m, with a height of 0.5 m from the top and bottom, respectively. Each internal chamber is identically equipped with a cooling agent distributor, a stripping agent distributor, a demister, five trays, and five secondary cyclone separators. Among them, the cooling agent distributor has a material nozzle on the lower surface, and the angle between the direction of the material nozzle and the axial direction of the vertical shell is 0°; the stripping agent distributor has a material nozzle on the upper surface; the angle between the direction of the material nozzle and the axial direction of the vertical shell is 0°; the demister is top-mounted; the tower plate is block-type; and the secondary cyclone separator is integrated.

[0205] The heavy hydrocarbon feedstock is divided into four groups, each with a flow rate of 28,000 kg / h. After being heated to 270°C in a feed preheater, each group is mixed with primary steam heated by a 22,400 kg / h dilution steam preheater through a controlled steam-to-hydrocarbon ratio, forming a 280°C vapor-to-hydrocarbon mixture. The vapor-to-hydrocarbon mixture enters the feed and cooling aid mixing distributor through vapor-to-hydrocarbon mixture inlet 2 of the gas-liquid separator. Diesel fuel at a temperature of 40°C enters the feed and cooling aid mixing distributor through cooling / washing aid pipeline c. The vapor-to-hydrocarbon mixture and cooling aid contact in the feed and cooling aid mixing distributor before entering the separation device. The angle α between the outlet of the feed and cooling aid mixing distributor and the axial direction of the housing is 0°. The weight ratio of diesel fuel to the vapor-to-hydrocarbon mixture is 0.05:1.

[0206] Water vapor at a temperature of 200°C enters the stripping agent inlet 5 of the separation device through the stripping agent pipeline d and then enters the gas-liquid separation device through the stripping agent distributor; wherein the angle β between the direction of the gas outlet and the axial direction is 0°; the weight ratio of water vapor as the stripping agent to the gas-hydrocarbon mixture is 0.05:1.

[0207] After the vapor-hydrocarbon mixture is brought into countercurrent contact with water vapor and diesel, it enters the cyclone separator 6 for preliminary separation treatment, and the resulting gaseous components enter the gas collection chamber through the gas phase outlet 1 of the cyclone separator 6; the resulting liquid phase components enter the tower tray 7 through the liquid phase outlet 3 of the cyclone separator 6 and the manifold, are further processed on the tower tray 7, and the resulting liquid phase components are sent to the liquid storage space 10 below; the gaseous phase products in the gas collection chamber are discharged through the gas phase outlet 1, and the four groups of liquid phase products are combined and sent to the cracking furnace for further processing. The four groups of liquid phase products in the liquid storage space 10 are discharged through the liquid phase outlet 3, combined and sent to the downstream device for further processing.

[0208] The average furnace outlet temperature of the device is set to 820℃. Under this cracking furnace outlet temperature balance and control, the fluctuation range of the average gasification rate of the gas phase summary main pipe of the gas-liquid separation device within 6 hours is shown in Table 1.

[0209] Example 2

[0210] The same as Example 1, except that one of the chambers is not provided with a cooling aid distributor and a stripping aid distributor.

[0211] The fluctuation range of the average gasification rate of the gas phase summary main pipe within 6 hours is shown in Table 1.

[0212] Example 3

[0213] The same as Example 1, except that one of the chambers is not provided with a demister and a tray.

[0214] The fluctuation range of the average gasification rate of the gas phase summary main pipe within 6 hours is shown in Table 1.

[0215] Example 4

[0216] The same as Example 1, except that the number of trays in one chamber is set to 15.

[0217] The fluctuation range of the average gasification rate of the gas phase summary main pipe within 6 hours is shown in Table 1.

[0218] Example 5

[0219] The same as Example 1, except that the number of cyclone separators in one chamber is set to 15.

[0220] The fluctuation range of the average gasification rate of the gas phase summary main pipe within 6 hours is shown in Table 1.

[0221] Example 6

[0222] The same as embodiment 1, except that one of the chamber cyclone separators is a three-stage cyclone separator.

[0223] The fluctuation range of the average gasification rate of the gas phase summary main pipe within 6 hours is shown in Table 1.

[0224] Example 7

[0225] The same as Example 1, except that the diameter of the tray arranged in one of the chambers is increased by 20%.

[0226] The fluctuation range of the average gasification rate of the gas phase summary main pipe within 6 hours is shown in Table 1.

[0227] Example 8

[0228] The same as embodiment 1, except that the volume of each cyclone separator arranged in one chamber is increased by 20%.

[0229] The fluctuation range of the average gasification rate of the gas phase summary main pipe within 6 hours is shown in Table 1.

[0230] Example 9

[0231] The same as Example 1, except that the diesel consumption in one chamber is increased by 10%.

[0232] The fluctuation range of the average gasification rate of the gas phase summary main pipe within 6 hours is shown in Table 1.

[0233] Example 10

[0234] The same as Example 1, except that the diesel temperature in one chamber is adjusted to 60°C.

[0235] The fluctuation range of the average gasification rate of the gas phase summary main pipe within 6 hours is shown in Table 1.

[0236] Example 11

[0237] The same as Example 1, except that the number of internal spaces is changed to 2, and the amount of heavy hydrocarbon feedstock and dilution steam is evenly distributed accordingly.

[0238] The fluctuation range of the average gasification rate of the gas phase summary main pipe within 6 hours is shown in Table 1.

[0239] Example 12

[0240] This is the same as Example 1, except that the shell gas phase outlet is connected to the downstream device, a single-hearth cracking furnace convection section. The cracking furnace has two sets of feedstock and two sets of cross-tubes. Each two cavity outlets of the shell are combined into one gas phase outlet, for a total of two gas phase outlets 1. The heavy hydrocarbon feedstock and dilution steam are evenly distributed accordingly.

[0241] The fluctuation range of the average gasification rate of the gas phase summary main pipe within 6 hours is shown in Table 1.

[0242] Example 13

[0243] The same as Example 1, except that the shell gas outlet is connected to the downstream device, a convection section of a dual-hearth cracking furnace. The cracking furnace has four feedstock feed groups and four cross-tube groups. Three of these groups feed heavy hydrocarbon feedstock with an API value of 40, and one group feeds conventional naphtha feedstock. The three inner cavity outlets for the heavy hydrocarbon feedstock are combined into a single gas outlet, while the inner cavity for the conventional naphtha feedstock has a separate gas outlet, for a total of two gas outlets.

[0244] The fluctuation range of the average gasification rate of the gas phase summary main pipe within 6 hours is shown in Table 1.

[0245] Example 14

[0246] A heavy hydrocarbon raw material with an API value of 40 is used; as shown in Figure 5, the vertical shell includes a top head, a large diameter cylinder, a first reduced diameter section, a small diameter cylinder, a second reduced diameter section and a bottom head from top to bottom. The total height of the shell is H = 8m, of which the inner cavity D1 of the large diameter cylinder is 5m, H1 = 5m, the inner cavity diameter D2 of the small diameter cylinder is 2.5m, and the inner cavity height H2 is 2m. The baffle height is 7m, and it is 0.5m away from the top and bottom of the shell respectively. Each internal space is configured in the same way, wherein each cavity of the large diameter cylinder is provided with a cooling agent distributor, a defoamer, and 5 secondary cyclone separators, and each cavity of the small diameter cylinder is provided with a stripping agent distributor and 5 tower plates. The rest is the same as in Example 1.

[0247] The fluctuation range of the average gasification rate of the gas phase summary main pipe within 6 hours is shown in Table 1.

[0248] Example 15

[0249] The same as Example 12, except that the tower tray set in the small-diameter cylinder is moved to the lower part of the large-diameter cylinder.

[0250] The fluctuation range of the average gasification rate of the gas phase summary main pipe within 6 hours is shown in Table 1.

[0251] Comparative Example 1

[0252] As shown in FIG3 , it is the same as Example 1, except that no baffle is provided in the gas-liquid separation device.

[0253] The fluctuation range of the average gasification rate of the gas phase summary main pipe within 6 hours is shown in Table 1.

[0254] Comparative Example 2

[0255] The same as Example 1, except that the four independent separation chambers are changed into four sets of gas-liquid separation devices in parallel. The volume of each device, the number of cyclone separators and the number of tower plates are the same as those of a single chamber configuration, and no baffle is set.

[0256] The fluctuation range of the average gasification rate of the gas phase summary main pipe within 6 hours is shown in Table 1.

[0257] As shown in Table 1, a comparison of the data in Examples 1-15 and Comparative Examples 1-2 shows that the flash separation apparatus is isolated into multiple, side-by-side separation chambers by the baffle 9. By increasing the number of cyclones or trays within each chamber, varying the size of the cyclones or trays, employing different cyclones or tray types, varying the flow rate and temperature of the stripping agent or cooling agent, or providing a reduced diameter section, the operation of each chamber can be precisely controlled, effectively reducing fluctuations in the outlet gasification rate, thereby controlling fluctuations in the feed rate into the radiant section furnace tubes and ensuring smooth operation of the cracking furnace. Under the conditions of the optimal embodiment, the fluctuation in the operating parameters of the gas-liquid separator can be reduced to a minimum of approximately 0.5%. All embodiments can extend the system life by at least 50% compared to the comparative example.

Claims

1. A method for producing olefins by steam cracking, comprising the following steps: 1) Heating heavy hydrocarbons to obtain a gas-liquid mixture, 2) transporting the gas-liquid mixture into a gas-liquid separation device for gas-liquid separation to obtain gas-phase material and liquid-phase material, wherein the gas-liquid separation device comprises: an inner cavity, which includes a top portion, an upper portion, a middle portion, a lower portion and a bottom portion, a liquid phase outlet, which is located at the bottom of the inner cavity and is configured to output the liquid phase material to the gas-liquid separation device, a gas phase outlet, which is located at the top of the inner cavity and is configured to output the gas phase material to the gas-liquid separation device, One or more baffles, which divide at least the middle part (preferably the upper part, the middle part and the lower part) of the inner cavity into n separation chambers along the central axis direction of the inner cavity, wherein each of the separation chambers includes an upper part, a middle part and a lower part, and n is an integer selected from 2-16 (preferably an integer selected from 4-8), a gas-liquid separation feeding device (preferably a gas-liquid separation feeding distributor), which is respectively arranged inside the n separation chambers and is configured to be able to transport the gas-liquid mixture into the n separation chambers, and gas-liquid separation components, which are respectively arranged inside the n separation chambers and are configured to respectively perform the gas-liquid separation in the n separation chambers to obtain corresponding n gas-phase materials and n liquid-phase materials, 3) optionally, combining at least two of the n gas phase materials together to form a comprehensive gas phase material, and optionally, combining at least two (preferably all) of the n liquid phase materials together to form a comprehensive liquid phase material, 4) steam cracking at least one (preferably all) of the n gaseous materials or the comprehensive gaseous materials to obtain a cracking product containing the olefin.

2. The method according to claim 1, wherein the gas-liquid separation component comprises at least one type selected from a gas-liquid enhanced contact device (preferably a tower tray), a centrifugal separation device (preferably a cyclone separator), a filtering device (preferably a demister), a stripping device (preferably a stripping aid distributor), a washing device (preferably a washing aid distributor) and a cooling device (preferably a cooling aid distributor), and the number of the gas-liquid separation components arranged in each of the separation chambers is independently selected from 0-20.

3. The method of claim 2, wherein the cooling aid is selected from at least one of liquid hydrocarbons and water vapor (preferably water vapor), the washing aid is selected from at least one of liquid hydrocarbons and water vapor (preferably light diesel), and the stripping aid is selected from at least one of gaseous hydrocarbons and water vapor (preferably water vapor).

4. The method of claim 2, wherein the gas-liquid separation feeding device is in fluid communication with the gas-liquid separation feed inlet, the cooling device is in fluid communication with the cooling aid inlet, the washing device is in fluid communication with the washing aid inlet, and the stripping device is in fluid communication with the stripping aid inlet.

5. The method according to claim 2, wherein the outlet of the gas-liquid separation feed distributor, the washing aid distributor or the cooling aid distributor is toward the lower part of the inner cavity and the angle between the direction of the outlet and the direction of the central axis of the inner cavity is 0-90° (preferably about 0°-30°), and the outlet of the stripping aid distributor is toward the upper part of the inner cavity and the angle between the direction of the outlet and the direction of the central axis of the inner cavity is 0-90° (preferably about 0°-30°).

6. The method of claim 2, wherein the number of the gas-liquid separation feeding devices (preferably gas-liquid separation feed distributors) in each separation chamber is independently selected from 1-5 (preferably 1-2), the number of the gas-liquid enhanced contact devices (preferably trays) in each separation chamber is independently selected from 0-20 (preferably 5-15), the number of the centrifugal separation devices (preferably cyclone separators) in each separation chamber is independently selected from 0-20 (preferably 5-15), the filtering devices (preferably demisters) The number of arrangements in each of the separation chambers is independently selected from 0-3 (preferably 1-2), the number of arrangements of the stripping devices (preferably stripping aid distributors) in each of the separation chambers is independently selected from 0-3 (preferably 1-2), the number of arrangements of the washing devices (preferably washing aid distributors) in each of the separation chambers is independently selected from 0-3 (preferably 1-2), or the number of arrangements of the cooling devices (preferably cooling aid distributors) in each of the separation chambers is independently selected from 0-3 (preferably 1-2).

7. The method of claim 1, wherein the gas-liquid separation component disposed inside the mth separation chamber is different from the gas-liquid separation component disposed inside the ith separation chamber, and m and i are different and are independently selected from integers from 1 to n.

8. The method of claim 7, wherein the gas-liquid separation components arranged inside the m-th separation chamber are different in number from the gas-liquid separation components arranged inside the ith separation chamber (preferably the difference in number is 1-4 or 1-2), or the gas-liquid separation components arranged inside the m-th separation chamber are different in type from the gas-liquid separation components arranged inside the ith separation chamber.

9. The method of claim 7, wherein the gas-liquid separation component arranged inside the mth separation chamber and the gas-liquid separation component arranged inside the ith separation chamber both include gas-liquid enhanced contact devices (preferably tower plates), but these devices differ in at least one indicator selected from the group consisting of setting quantity, separation efficiency, separation principle, operating parameters, device structure and size specifications.

10. The method according to claim 7, wherein the gas-liquid separation component arranged inside the mth separation chamber and the gas-liquid separation component arranged inside the ith separation chamber both include centrifugal separation devices (preferably cyclone separators), but these devices differ in at least one indicator selected from the group consisting of setting quantity, separation efficiency, separation principle, device structure and size specifications.

11. The method of claim 7, wherein the gas-liquid separation component arranged inside the mth separation chamber and the gas-liquid separation component arranged inside the ith separation chamber both include a filtering device (preferably a demister), but these devices differ in at least one indicator selected from the group consisting of the number of settings, separation efficiency, separation principle, device structure and size specifications.

12. The method of claim 7, wherein the gas-liquid separation component arranged inside the mth separation chamber and the gas-liquid separation component arranged inside the i-th separation chamber both include a stripping device (preferably a stripping agent distributor), but these devices differ in at least one indicator selected from the group consisting of the number of settings, separation efficiency, separation principle, device structure and size specifications.

13. The method according to claim 7, wherein the gas-liquid separation component arranged inside the mth separation chamber and the gas-liquid separation component arranged inside the ith separation chamber both include a washing device (preferably a washing aid distributor), but these devices differ in at least one indicator selected from the group consisting of setting quantity, separation efficiency, separation principle, device structure and size specifications.

14. The method of claim 7, wherein the gas-liquid separation component arranged inside the mth separation chamber and the gas-liquid separation component arranged inside the ith separation chamber both include a cooling device (preferably a cooling aid distributor), but these devices differ in at least one indicator selected from the group consisting of setting quantity, separation efficiency, separation principle, device structure and size specifications.

15. The method of claim 1, wherein a washing device (preferably a washing aid distributor) or a cooling device (preferably a cooling aid distributor) is arranged at the top and / or upper part of the inner cavity, or a stripping device (preferably a stripping aid distributor) is arranged at the lower part and / or bottom of the inner cavity.

16. The method according to claim 1, wherein a plurality of the baffles are provided, and the angle between two adjacent baffles is 0-180° (preferably 30-90°).

17. The method of claim 1, wherein the baffle is longitudinally arranged inside the inner cavity along the central axis direction of the inner cavity, and the longitudinal edge of the baffle is sealed to the inner wall of the inner cavity so that the n separation chambers form independent chambers.

18. The method of claim 1, wherein the upper edge of at least one of the baffles is sealed and connected to the side wall of the top of the inner cavity. Preferably, there is a gap (called the first gap) between the upper edge of at least one of the baffles and the side wall of the top of the inner cavity, thereby enabling the upper fluids of the n separation chambers to be connected, forming an air collecting chamber together with the top space of the inner cavity.

19. The method of claim 1, wherein there is a gap (called a second gap) between the lower edge of the baffle and the side wall of the bottom of the inner cavity, thereby connecting the lower fluids of the n separation chambers to form a liquid storage space together with the bottom space of the inner cavity.

20. The method of claim 2, wherein the cyclone separator is disposed at the upper portion of the separation chamber, and the tower tray is disposed below the cyclone separator (for example, disposed in the middle or lower portion of the separation chamber).

21. The method of claim 2, wherein the gas-liquid separation device is further provided with a collecting pipe, wherein the liquid phase inlet of the collecting pipe is fluidically connected to the liquid phase outlet of the cyclone separator, and the liquid phase outlet of the collecting pipe is fluidically connected to the upper side of the tower plate.

22. The method of claim 1, wherein a sealing cover plate is horizontally arranged on the top of the inner cavity, and a periphery of the sealing cover plate is sealedly connected to a side wall of the inner cavity so that an internal space of the inner cavity located above the sealing cover plate forms an air collecting chamber, and a plurality of openings are arranged on the sealing cover plate so that an internal space of the inner cavity located below the sealing cover plate is fluidically connected to the air collecting chamber via the plurality of openings.

23. The method of claim 22, wherein an upper edge of at least one (preferably all) of the baffles is sealingly connected to a lower surface of the sealing cover plate, thereby arranging the n separation chambers in an inner space of the inner cavity below the sealing cover plate.

24. The method of claim 22, wherein the opening of the sealing cover plate is in fluid communication with a gas phase outlet of the cyclone separator so that the gas phase separated by the cyclone separator can enter the gas collecting chamber.

25. The method of claim 22, wherein a downcomer is also provided in the gas-liquid separation device, wherein at least one of the openings of the sealing cover plate is fluidly connected to the downcomer so as to transport the liquid collected on the sealing cover plate to the internal space below the sealing cover plate (preferably to the liquid storage space) via the downcomer.

26. The method of claim 1, wherein the inner cavity is surrounded by a vertical shell, and the vertical shell is a cylindrical shell, wherein the cylindrical shell includes a top head, a cylinder with a constant diameter, and a bottom head from top to bottom, or the cylindrical shell includes a top head, a large-diameter cylinder, a first reduced-diameter section, a small-diameter cylinder, a second reduced-diameter section, and a bottom head from top to bottom.

27. The method of claim 26, wherein the inner cavity diameter D of the equal-diameter cylinder is 3-10m, and the inner cavity height H is 5-12m, the inner cavity diameter D1 of the large-diameter cylinder is 3-10m, and the inner cavity height H1 is 3-8m, and the inner cavity diameter D2 of the small-diameter cylinder is 1-5m, and the inner cavity height H2 is 1-4m.

28. The method of claim 1, wherein the lower edge of the baffle extends to the small diameter cylinder, and / or the cyclone separator is arranged on the upper part of the large diameter cylinder, and the tower plate is arranged on the upper part or middle part of the small diameter cylinder.

29. The method of claim 1, wherein the final distillation point temperature of the heavy hydrocarbon is above 540°C (preferably the initial distillation point temperature is 15°C and the final distillation point temperature is above 750°C), and / or the API value of the heavy hydrocarbon is not less than 32 (preferably above 38), and / or the heavy hydrocarbon is selected from at least one of paraffin-based crude oil, intermediate-based crude oil, cycloalkyl crude oil, condensate oil and refined products.

30. The method of claim 1, wherein in step 1), the heavy hydrocarbon is heated to 100-400°C (preferably 200-370°C).

31. The method of claim 1, wherein in the n separation chambers, the operating temperature of the gas-liquid separation is independently 100-400°C (preferably 200-370°C), and the operating pressure of the gas-liquid separation is independently 0.4-0.7 MPaG.

32. The method of claim 1, wherein in step 4), at least one performance indicator of the gas phase material or the comprehensive gas phase material is monitored, and the operating parameters of at least one of the n separation chambers are maintained or changed based on the monitoring results.

33. The method of claim 32, wherein the performance index is selected from at least one of the vapor phase final distillation point, the liquid phase final distillation point, the vapor phase heavy component content, the liquid phase light component content and the vaporization rate, and the operating parameter is selected from at least one of the gas-liquid mixture temperature, the gas-liquid mixture pressure, the gas-liquid mixture flow rate, the gas-liquid mixture distributor linear velocity, the cooling aid temperature, the cooling aid pressure, the cooling aid flow rate, the cooling aid distributor linear velocity, the washing aid temperature, the washing aid pressure, the washing aid flow rate, the washing aid distributor linear velocity, the stripping aid temperature, the stripping aid pressure, the stripping aid flow rate and the stripping aid distributor linear velocity.

34. A gas-liquid separation device, comprising: an inner cavity, which includes a top portion, an upper portion, a middle portion, a lower portion and a bottom portion, a liquid phase outlet, which is located at the bottom of the inner cavity, a gas phase outlet, which is located at the top of the inner chamber, One or more baffles, which divide at least the middle part (preferably the upper part, the middle part and the lower part) of the inner cavity into n separation chambers along the central axis direction of the inner cavity, wherein each of the separation chambers includes an upper part, a middle part and a lower part, a gas-liquid separation feeding device (preferably a gas-liquid separation feeding distributor), which is respectively arranged inside the n separation chambers, a gas-liquid separation component, which is configured to realize a gas-liquid separation function and is respectively arranged inside the n separation chambers, Among them, the gas-liquid separation component arranged inside the mth separation chamber is different from the gas-liquid separation component arranged inside the ith separation chamber, n is an integer selected from 2-10 (preferably an integer selected from 3-6), m and i are different, and each is independently selected from integers from 1 to n.

35. A gas-liquid separation method, comprising the step of conveying a gas-liquid separation feed through a gas-liquid separation feed device (preferably a gas-liquid separation feed distributor) into the gas-liquid separation device of claim 34 to perform gas-liquid separation.

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