System for treating heavy hydrocarbon

Abstract

The invention relates to a system for treating heavy hydrocarbon, which can reduce the content of heavy fraction impurities in a gas-phase component and the content of light components in a liquid-phase component by injecting a cooling aid, a separation aid and an optional gas stripping aid, thereby improving the gas-liquid separation effect. Moreover, the flash separation equipment is separated into a plurality of separation chambers which are arranged side by side through baffles, each separation chamber is provided with a steam-hydrocarbon mixture inlet and a gas phase outlet, and a high-temperature steam-hydrocarbon mixture entering the separation chamber is separated and then directly enters a downstream device from the gas phase outlet of the separation chamber. The hydrocarbon partial pressure can be adjusted without arranging a high-temperature adjusting valve on the gas phase outlet pipeline, so that the fault rate of the high-temperature adjusting valve at high temperature can be reduced, and the service life of the system can be prolonged. In addition, a cyclone hydraulic separator and a tower tray are arranged in each separation chamber, so that the gas-liquid separation efficiency and the flash evaporation effect can be improved.

Description

Technical Field

[0001] The present disclosure relates to the field of petrochemical engineering, and in particular, to a system for processing heavy hydrocarbons. Background Art

[0002] At present, the world's oil demand is declining year by year with the development of new energy, and at the same time, there is an oversupply of refining capacity. Therefore, how to study the efficient and short-process utilization of crude oil, reduce the investment and energy consumption of crude oil utilization equipment, and improve the economic benefits of equipment has become a common concern of the global refining industry.

[0003] To this end, domestic and foreign scholars have developed a flash evaporation method to apply crude oil to the fields of 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. The principle of flash evaporation is to reduce the pressure of high-pressure and high-temperature fluid to lower its boiling point. At this time, the high-temperature liquid near the boiling point under high pressure is reduced in pressure to lower its boiling point. The liquid absorbs its own energy and partially vaporizes to form a new vapor-liquid equilibrium, that is, the fluid temperature is higher than the boiling point under the pressure, the fluid boils and vaporizes rapidly, and the two phases are separated.

[0004] Since the separation efficiency of conventional flash tanks is extremely low, and the equipment is large and occupies a lot of space, great progress has been made through the continuous in-depth research of domestic and foreign scholars. At present, crude oil flash treatment mainly focuses on the following aspects: optimizing the vacuum pumping system to improve the vacuum degree at the top of the container tower; using new and efficient fillers and direct contact heat transfer methods to reduce the total pressure drop of the container and maintain a high vacuum degree in the flash section; optimizing the design and operation of the washing section and strengthening the fractionation concept of the washing section; developing new and efficient gas and liquid distributors; using enhanced crude oil distillation methods, etc.

[0005] CN03815733.0 discloses a steam cracking method for heavy hydrocarbon raw materials, wherein the raw materials are prepared by mixing preheated heavy hydrocarbons with water and dilution steam to form a mixed stream, and then passing through a flash tank to separate the vapor phase from the liquid phase. The vapor phase is then passed through a separator to further remove non-volatiles, and the gas phase product finally obtained enters a cracking furnace for cracking. In order to reduce and avoid the coking problem, the invention controls the constant hydrocarbon partial pressure by arranging a regulating valve on the pipeline between the separator outlet and the convection section of the cracking furnace. However, the method is complicated to operate, and is simply combined with a tank body and a valve group, without fundamentally improving the gas-liquid separation efficiency in terms of process technology. In addition, the cracking furnace usually has multiple groups of feed pipelines, and the material temperature in the pipeline between the separator outlet and the convection section of the cracking furnace is very high. Arranging a regulating valve group on the pipeline requires a relatively large device investment, and increases the probability of failure under long-term high-temperature environment operation, affecting long-term operation. Summary of the invention

[0006] The purpose of the present disclosure is to provide a system for processing heavy hydrocarbons, in order to solve the problems of low gas-liquid separation efficiency, poor flash evaporation effect and difficulty in long-term operation that occur in the prior art.

[0007] In order to achieve the above-mentioned object, the present disclosure provides a system for processing heavy hydrocarbons, which includes a separation device; the separation device includes a vertical shell, a tower tray arranged inside the vertical shell, a hydrocyclone separator arranged inside the vertical shell, a liquid storage space and an optional baffle; the hydrocyclone separator is arranged at the upper part of the vertical shell, the tower tray is arranged in the middle part of the vertical shell and below the hydrocyclone separator, and the liquid storage space is arranged at the lower part or outside of the vertical shell; the baffle is arranged vertically inside the vertical shell and the edge of the baffle is sealed and connected to the inner wall of the vertical shell. The upper space in the shell is divided into a plurality of separation chambers arranged side by side; the separation device comprises a vapor-hydrocarbon mixture inlet, a cooling / separation aid injection inlet, a gas phase outlet, a liquid phase outlet and an optional gas stripping agent inlet; the vapor-hydrocarbon mixture inlet of the separation device is used to communicate with a heavy hydrocarbon source; the cooling / separation aid inlet of the separation device is used to communicate with a cooling aid source or a separation aid source; the gas stripping agent inlet of the separation device is used to communicate with a gas stripping agent source; the gas phase outlet of the separation device is used to communicate with a gas phase downstream device; and the liquid phase outlet of the separation device is used to communicate with a liquid phase downstream device.

[0008] Optionally, the separation chamber includes a cyclone separator, a tower tray and a liquid storage space which are arranged in sequence from top to bottom; the cyclone separator is arranged in the upper space of the separation chamber, so that the vapor-hydrocarbon mixture entering the separation chamber is flashed to obtain a gas phase component and a liquid phase component, and the gas phase component enters the cyclone separator for separation to further separate the entrained liquid phase component; a cooling / separation aid storage or distributor is arranged below the inlet of the upper cyclone separator of the separation chamber, so that the gas phase component obtained by the 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 separation aid and enter the tower tray below for further separation; the tower tray is arranged in the middle of the separation chamber and below the cyclone separator, so that the liquid phase component separated by the cyclone separator in the separation chamber can be further separated by the tower tray; the liquid storage space is arranged in the lower space of the separation chamber, so that the liquid phase component further separated by the tower tray in the separation chamber can flow into the liquid storage space.

[0009] Optionally, a sealing cover plate is further provided in the separation chamber; the sealing cover plate is horizontally arranged above the cyclone separator and the edge of the sealing cover plate is tightly combined with the side wall of the separation chamber, so that the upper space of the sealing cover plate forms an air collecting chamber; a gas phase opening is provided on the sealing cover plate and the gas phase opening is connected to the gas phase outlet of the cyclone separator, so that the gas phase separated by the cyclone separator can enter the gas collecting chamber.

[0010] Optionally, a collecting pipe is further provided in the separation chamber; the collecting pipe comprises a liquid phase inlet and a liquid phase outlet, the liquid phase inlet of the collecting pipe is connected to the liquid phase outlet of the cyclone separator, and the liquid phase outlet of the collecting pipe extends to the inlet of the tower plate.

[0011] Optionally, the number of stages of the hydrocyclone separator inside the separation chamber is 2 or more.

[0012] Optionally, a gas phase outlet is provided at the top of the separation chamber for communicating with a gas phase downstream device; a liquid phase outlet is provided at the bottom of the separation chamber for communicating with a liquid phase downstream device; a vapor-hydrocarbon mixture inlet, a cooling / separation aid inlet and an optional gas stripping aid inlet are also provided on the side wall of the separation chamber; the vapor-hydrocarbon mixture inlet of the separation chamber is used to communicate with a heavy hydrocarbon source; the cooling / separation aid inlet of the separation chamber is used to communicate with a cooling aid source or a separation aid source; and the gas stripping aid inlet of the separation chamber is used to communicate with a gas stripping aid source.

[0013] Optionally, the separation chamber further includes a feed and cooling agent mixing distributor and a gas stripping agent distributor; the two inlets of the feed and cooling agent mixing distributor extend to the outside of the separation chamber to form the steam-hydrocarbon mixture inlet and the cooling / separation agent inlet respectively; the inlet of the gas stripping agent distributor extends to the outside of the separation chamber to form the gas stripping agent inlet; the outlet of the feed and cooling agent 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 to 90°; the outlet of the gas stripping agent distributor is arranged toward the upper part of the vertical shell, and the direction of the outlet is the same as the axial direction of the vertical shell. The angle β between the axial directions of the shell is 0 to 90°; or, the separation chamber also includes a separation aid distributor and a feed distributor; the inlet of the separation aid distributor extends to the outside of the separation chamber to form the cooling / separation aid inlet; the inlet of the feed distributor extends to the outside of the separation chamber to form the vapor-hydrocarbon mixture inlet; the outlet of the separation 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 to 90°; 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 to 90°.

[0014] Optionally, the angle between two adjacent baffles is 0 to 180°.

[0015] Optionally, the system further comprises a raw material pipeline, a cooling / separation agent pipeline and an optional steam stripping agent pipeline; the inlet of the raw material pipeline is connected to the heavy hydrocarbon source, and the outlet is connected to the steam-hydrocarbon mixture inlet of the vertical shell; the inlet of the cooling / separation agent pipeline is connected to the cooling agent source or the separation agent source, and the outlet is connected to the cooling / separation agent inlet of the vertical shell; the inlet of the stripping agent pipeline is connected to the stripping agent source, and the outlet is connected to the stripping agent inlet of the vertical shell; a feed preheater is provided on the raw material pipeline for heating the material in the raw material pipeline; the feed preheater is selected from one or more of a heating furnace, a cracking furnace convection section and a heat exchanger.

[0016] Optionally, the system also includes a steam pipeline; a primary steam inlet and a secondary steam inlet are provided on the raw material pipeline; a secondary steam inlet is provided on the gas stripping agent pipeline; the steam pipeline can be divided into a primary steam pipeline and a secondary steam pipeline; the inlets of the primary steam pipeline and the secondary steam pipeline are used to communicate with a steam source; the outlet of the primary steam pipeline is connected to the primary steam inlet on the raw material pipeline; the outlet of the secondary steam pipeline is connected to the secondary steam inlets on the raw material pipeline and the gas stripping agent pipeline; steam preheaters are provided on the primary steam pipeline and the secondary steam pipeline for heating steam; the steam preheater is selected from one or more of a heating furnace, a cracking furnace convection section and a heat exchanger.

[0017] Through the above technical scheme, the present disclosure can reduce the content of heavy fractions and impurities such as colloids in the gas phase component by injecting cooling aids, separation aids and optional gas stripping aids, thereby improving the effect of gas-liquid separation, avoiding coking in the radiation section, and thus extending the decoking cycle of the cracking furnace; on the other hand, it can reduce the content of light components in the liquid phase component. Among them, injecting separation aids or gas stripping aids can maximize the gasification of light components in the liquid phase component to obtain light components to the maximum extent; injecting cooling aids can control the gasification rate and reduce the entrainment of heavy components, while increasing the liquid phase flow rate to improve the separation effect of the tower plate. In addition, the present disclosure isolates the flash separation equipment into multiple separation chambers arranged side by side through baffles, each separation chamber is provided with a raw material inlet and a gas phase outlet, and the high-temperature gas-hydrocarbon mixture entering the separation chamber directly enters the downstream device from the gas phase outlet of the above separation chamber after separation, without the need to adjust the hydrocarbon partial pressure by setting a high-temperature regulating valve on the gas phase outlet pipeline, which can reduce the failure rate of the high-temperature regulating valve at high temperature, thereby improving the life of the system. In addition, a cyclone separator and a tray are provided in each separation chamber, which can improve the gas-liquid separation efficiency and the flash evaporation effect to further reduce the entrainment of heavy components and impurities such as colloids, and avoid their coking in the radiation section, thereby further extending the decoking cycle of the cracking furnace.

[0018] Other features and advantages of the present disclosure will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0019] The accompanying drawings are used to provide a further understanding of the present disclosure and constitute a part of the specification. Together with the following specific embodiments, they are used to explain the present disclosure but do not constitute a limitation of the present disclosure. In the accompanying drawings:

[0020] Figure 1 Schematic diagram of a system for processing heavy hydrocarbons in Example 1 of the present disclosure.

[0021] Figure 2 Schematic diagram of a system for processing heavy hydrocarbons in Example 2 of the present disclosure.

[0022] Figure 3 is a front view of the flash separation device used in Comparative Example 1 of the present disclosure.

[0023] Figure 4 It is a top view of a flash separation device disclosed in the present invention.

[0024] Description of Reference Numerals

[0025] 1. Gas phase outlet; 2. Gas-hydrocarbon mixture inlet; 3. Liquid phase outlet; 4. Cooling / separation agent inlet; 5. Gas stripping agent inlet; 6. Hydrocyclone separator; 7. Tower tray; 8. Sealing cover plate; 9. Baffle; 10. Liquid storage space;

[0026] a, raw material pipeline; b, steam pipeline; b1, primary steam pipeline; b2, secondary steam pipeline; c, cooling / separation auxiliary agent pipeline; d, gas stripping auxiliary agent pipeline. DETAILED DESCRIPTION

[0027] The specific implementation of the present disclosure is described in detail below in conjunction with the accompanying drawings. It should be understood that the specific implementation described herein is only used to illustrate and explain the present disclosure, and is not used to limit the present disclosure.

[0028] In the present disclosure, unless otherwise stated, directional words such as "upper" and "lower" generally refer to the upper and lower parts of a device in normal use. Figure 1 In the drawing direction, "inside" and "outside" refer to the outline of the device. In addition, the terms "first" and "second" are used for descriptive purposes only and cannot be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Therefore, the features defined as "first" and "second" may explicitly or implicitly include one or more of the features. In the description of the present disclosure, the meaning of "multiple" is two or more, unless otherwise clearly and specifically defined.

[0029] like Figure 1As shown, the present disclosure provides a system for processing heavy hydrocarbons, which includes a separation device; the separation device includes a vertical shell, a tower tray 7 arranged inside the vertical shell, a hydrocyclone 6 arranged inside the vertical shell, a liquid storage space 10 and an optional baffle 9; the hydrocyclone 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 hydrocyclone 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 and connected to 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 / separation aid inlet 4, a gas phase outlet 1, A liquid phase outlet 3 and an optional gas stripping agent inlet 5; the vapor-hydrocarbon mixture inlet 2 of the separation device is used to communicate with a heavy hydrocarbon source so that the vapor-hydrocarbon mixture can enter the separation device for gas-liquid separation; the cooling / separation agent inlet 4 of the separation device is used to communicate with a cooling agent source or a separation agent source so that a cooling agent or a separation agent can enter the separation device to cool or separate the vapor-hydrocarbon mixture; the gas stripping agent inlet 5 of the separation device is used to communicate with a gas stripping agent source so that the gas stripping agent can enter the separation device for gas stripping treatment; the gas phase outlet 1 of the separation device is used to communicate with a 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 a liquid phase downstream device so that the separated liquid phase components can enter the liquid phase downstream device for further use.

[0030] Through the above technical scheme, the present disclosure can reduce the content of heavy fractions and impurities such as colloids in the gas phase component by injecting cooling aids, separation aids and optional gas stripping aids, thereby improving the effect of gas-liquid separation, avoiding coking in the radiation section, and thus extending the decoking cycle of the cracking furnace; on the other hand, it can reduce the content of light components in the liquid phase component. Among them, injecting separation aids or gas stripping aids can maximize the gasification of light components in the liquid phase component to obtain light components to the maximum extent; injecting cooling aids can control the gasification rate and reduce the entrainment of heavy components, while increasing the liquid phase flow rate to improve the separation effect of the tower plate. In addition, the present disclosure isolates the flash separation equipment into multiple separation chambers arranged side by side through baffles, each separation chamber is provided with a raw material inlet and a gas phase outlet, and the high-temperature gas-hydrocarbon mixture entering the separation chamber directly enters the downstream device from the gas phase outlet of the above separation chamber after separation, without the need to adjust the hydrocarbon partial pressure by setting a high-temperature regulating valve on the gas phase outlet pipeline, which can reduce the failure rate of the high-temperature regulating valve at high temperature, thereby improving the life of the system. In addition, a cyclone separator and a tray are provided in each separation chamber, which can improve the gas-liquid separation efficiency and the flash evaporation effect to further reduce the entrainment of heavy components and impurities such as colloids, and avoid their coking in the radiation section, thereby further extending the decoking cycle of the cracking furnace.

[0031] Among them, the cooling aid, separation aid and gas 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 or light diesel.

[0032] Among them, the vertical shell is a conventional choice in the field, and the present application can reasonably select according to different needs. For example, the vertical shell can be a cylinder of equal diameter 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.

[0033] Wherein, the gas phase outlet 1 is arranged at the top of the vertical shell, and is used to communicate 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, and is used to communicate 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 / separation aid inlet 4 and the optional gas stripping aid inlet 5 are arranged on the side of the above-mentioned vertical shell, and 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 / separation aid inlet 4 is used to communicate with the cooling aid source or the separation aid source, so that the cooling aid or the separation aid can enter the separation device to participate in the separation process; the gas stripping aid inlet 5 is used to communicate with the gas stripping aid source, so that the gas stripping aid can enter the separation device to participate in the separation process.

[0034] Among them, preferably, the vapor-hydrocarbon mixture inlet 2 of the separation device can be arranged on the same horizontal line as the cooling / separation aid inlet 4. In this case, the separation device is provided with a gas stripping aid inlet 5 and the gas 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 / separation aid inlet 4. In this case, the separation device is not provided with a gas stripping aid inlet 5.

[0035] The system further comprises a raw material pipeline a, a cooling / separation agent pipeline c and an optional gas stripping agent 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 / separation agent pipeline c is connected to the cooling agent source or the separation agent source, and the outlet is connected to the cooling / separation agent inlet 4 of the vertical shell, so that the cooling agent or the separation agent can enter the separation device through the cooling / separation agent pipeline c; the inlet of the gas stripping agent pipeline d is connected to the gas stripping agent source, and the outlet is connected to the gas stripping agent inlet 5 of the vertical shell, so that the gas stripping agent can enter the separation device through the gas stripping agent pipeline d; a feed preheater is provided on the raw material pipeline a for heating the material in the raw material pipeline a. In addition, a raw material branch line is also arranged 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 arrangement of the raw material branch line, the temperature of the raw material entering the separation device can be flexibly adjusted.

[0036] The system further comprises a steam pipeline b; a primary steam inlet and a secondary steam inlet are provided on the raw material pipeline a; a secondary steam inlet is provided on the stripping agent pipeline d; 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 to 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, so that the temperature of the steam can be flexibly adjusted.

[0037] Wherein, 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.

[0038] The steam entering the steam pipeline b includes one of dilution steam, low-pressure steam, medium-pressure steam or high-pressure steam.

[0039] In the above embodiment, 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, so that the phase state and temperature of the steam-hydrocarbon mixture transported to the flash separation device can be flexibly controlled, and then the separation effect of the flash separation can be flexibly controlled.

[0040] In one embodiment, the baffle 9 may not be provided in the vertical shell, and the entire shell contains only one cavity.

[0041] In another embodiment, in order to improve the life and separation effect of the separation device, it is necessary to set a plurality of baffles 9 in the vertical housing so that the interior of the vertical housing is divided into a plurality of separation chambers arranged side by side. The angle between two adjacent baffles 9 is 0 to 180°, preferably 60 to 120°, and more preferably 90°; for example, in a specific embodiment of the present disclosure, Figure 3 As shown, the flash separation device comprises four baffles 9, and the angle between two adjacent baffles 9 is 90°, dividing the internal space of the vertical shell into four separation chambers of the same size.

[0042] 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 the subsequent gas phase downstream device.

[0043] 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 the subsequent liquid phase downstream device.

[0044] Among them, a vapor-hydrocarbon mixture inlet 2, a cooling / separation aid inlet 4 and an optional gas stripping aid inlet 5 are also 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 / separation aid inlet 4 of the separation chamber is used to communicate with a cooling aid source or a separation aid source; the gas stripping aid inlet 5 of the separation chamber is used to communicate with a gas stripping aid source; so that the vapor-hydrocarbon mixture, the cooling aid and the gas stripping aid can enter the separation device through the vapor-hydrocarbon mixture inlet 2, the cooling / separation aid inlet 4 and the gas stripping aid inlet 5 respectively to participate in the separation process.

[0045] In order to further improve the gas-liquid separation effect, the relative position relationship of the steam-hydrocarbon mixture inlet 2, the cooling / separation aid inlet 4 and the optional stripping aid inlet 5 is reasonably set. For example, the position relationship between the various inlets can be that the steam-hydrocarbon mixture inlet 2 and the cooling / separation aid inlet 4 are on the same horizontal line, and the stripping aid inlet 5 is set below; or the cooling / separation aid inlet 4, the steam-hydrocarbon mixture inlet 2 and the stripping aid inlet 5 are set in sequence from top to bottom; or the cooling / separation aid inlet 4 and the steam-hydrocarbon mixture inlet 2 are set in sequence from top to bottom. Whether to set the stripping aid inlet, the cooling / separation aid inlet 4 to inject the cooling aid or the separation aid and the position relationship between the various inlets need to be determined according to the properties of the heavy hydrocarbon feedstock and the operating procedures.

[0046] Wherein, when the vapor-hydrocarbon mixture inlet 2 and the cooling / separation aid inlet 4 are at the same horizontal line, the feed device connected to the vapor-hydrocarbon mixture inlet 2 and the feed device connected to the cooling / separation 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 / separation aid inlet 4 can be evenly mixed in the linking assembly.

[0047] The cooling / separation aid inlet 4 and the vapor-hydrocarbon mixture inlet 2 are both arranged below the inlet of the hydrocyclone 6. In this embodiment, the problem that the vapor-hydrocarbon mixture, the cooling aid and the separation aid enter the hydrocyclone 6 and affect the gas-liquid separation effect can be avoided.

[0048] like Figure 1As shown, when the vapor-hydrocarbon mixture inlet 2 and the cooling / separation aid inlet 4 are at the same horizontal line, they are both arranged below the inlet of the cyclone separator 6; the stripping agent inlet 5 is arranged below and between the liquid storage space 10 and the tower plate 7, and the separation chamber also includes a feed and cooling agent mixing distributor and a stripping agent distributor.

[0049] Among them, 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 / separation 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 to 90°.

[0050] 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 outlet and the axial direction of the vertical shell is 0 to 90°.

[0051] In this embodiment, the vapor hydrocarbon mixture and the cooling aid enter the feed and cooling aid mixing distributor through both ends of the feed and cooling aid mixing distributor and mix, so that the vapor hydrocarbon mixture can be preliminarily condensed; the preliminarily condensed material enters the separation chamber through the outlet of the distributor. The gas stripping medium distributor can spray the gas stripping aid upward and fully contact with the preliminarily condensed material above, further enhancing the gas stripping effect, and further enhancing the gas-liquid separation effect and separation efficiency.

[0052] like Figure 2 As shown, when the cooling / separation aid inlet 4 and the steam-hydrocarbon mixture inlet 2 are arranged in sequence from top to bottom, the separation chamber further includes a feed distributor and a separation aid distributor.

[0053] 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 outlet and the axial direction of the vertical shell is 0 to 90°.

[0054] Among them, the inlet of the separation aid distributor extends to the outside of the separation chamber to form the cooling / separation aid inlet 4; the outlet of the separation 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 to 90°.

[0055] In the above embodiment, 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 separation aid distributor can make the separation aid flow downward, so that the separation aid can fully contact with the vapor-hydrocarbon mixture, which can effectively prevent the entrainment of heavy fractions and impurities in the gas phase components, and avoid entering the downstream device to cause coking and other phenomena; wherein the heavy fractions and impurities include one or more of colloids, asphaltene, metal impurities, sulfur, oxygen, nitrogen and heavy components. In addition, the feed distributors, cooling aid distributors and gas lift distributors in multiple separation chambers can be set at the same or different heights, depending on the temperature and pressure of the vapor-hydrocarbon mixture.

[0056] Among them, the feed distributor, feed and cooling agent mixing distributor, separation agent distributor and gas stripping agent distributor are provided with multiple open areas as distributor outlets; the open area porosity is 5-15%, and the average pore size of the open areas is 10-20 mm.

[0057] Wherein, the cooling / separation auxiliary agent inlet includes a liquid hydrocarbon inlet and / or a water inlet; the gas stripping auxiliary agent inlet includes a liquid hydrocarbon inlet and / or a water inlet.

[0058] The separation chamber includes a hydrocyclone separator 6, a tray 7 and a liquid storage space 10 arranged in sequence from top to bottom;

[0059] like Figure 1 As shown, 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 plate 7 is arranged in the middle of the separation chamber and 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 plate 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 plate 7 in the separation chamber can flow into the liquid storage space 10.

[0060] The liquid storage space 10 may be independently arranged outside the separation chamber.

[0061] The tray 7 and hydrocyclone 6 used in the present disclosure are conventional choices in the art, and this application does not make any special requirements.

[0062] Wherein, a collecting pipe is also 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 plate 7.

[0063] In this embodiment, 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 feed 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.

[0064] Wherein, the number of stages of the hydrocyclones 6 inside the separation chamber is one or more; when the number of stages of the hydrocyclones 6 inside each of the separation chambers is one, the lower end outlet of the hydrocyclones 6 is connected to the inlet of the manifold, so that the liquid separated by the above-mentioned hydrocyclones can enter the liquid collection area below through the manifold. If the number of stages of the hydrocyclones 6 inside each of the separation chambers is , there is a gap between the outer walls of the material legs of the multiple hydrocyclones 6, and the length of the material legs of the multiple hydrocyclones 6 increases from the outside to the inside; the lower end outlets of the multiple hydrocyclones 6 are all connected to the inlet of the manifold, so that all the liquid separated by the above-mentioned multiple hydrocyclones can enter the tower plate 7 below through the manifold.

[0065] Wherein, a cooling / separation aid storage or distributor is arranged 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 separation aid and enter the tower plate below for further separation.

[0066] In each of the separation chambers, a sealing cover plate 8 is also provided; the sealing cover plate 8 is horizontally arranged above the hydrocyclone 6 and the edge of the sealing cover plate 8 is tightly combined with the side wall of the separation chamber, so that the upper space of the sealing cover plate 8 forms a gas collecting 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 hydrocyclone 6, so that the gas phase separated by the hydrocyclone 6 can enter the gas collecting chamber. In this embodiment, by providing the sealing cover plate 8, the gas phase components in the separation chamber can be discharged from the separation device only through the gas phase outlet 1 of the hydrocyclone 6, further improving the effect of gas-liquid separation.

[0067] In one embodiment, the operating conditions of the separation device disclosed herein are conventionally selected in the art and need to be determined based on the properties of the materials in each separation chamber.

[0068] In one embodiment, the heavy hydrocarbon feedstock used in the present disclosure is conventionally selected in the art, and this application does not make special requirements. For example, the heavy hydrocarbon feedstock is selected from heavy hydrocarbons with an API value of 22 or above.

[0069] like Figure 1 As shown, the method for treating heavy hydrocarbons using the system of the present disclosure includes:

[0070] The heavy hydrocarbon feedstock is heated to 200-400°C in a feed preheater and then mixed with primary dilution steam heated to 180-400°C in a dilution steam preheater to form a vapor-hydrocarbon mixture at 150-350°C; the vapor-hydrocarbon mixture enters the feed and cooling agent mixing distributor through the vapor-hydrocarbon mixture inlet 2 of the flash separation device; the cooling agent enters the other end of the feed and cooling agent mixing distributor through the cooling / separation agent pipeline c; the vapor-hydrocarbon mixture and the cooling agent contact in the feed and cooling agent mixing distributor and then enter the separation device; wherein the angle α between the direction of the outlet of the feed and cooling agent mixing distributor and the axial direction of the shell is 0-90°; the cooling agent is selected from liquid hydrocarbons and / or water;

[0071] The stripping agent enters the stripping agent inlet 5 of the separation device through the stripping agent pipeline d and then enters the flash separation device through the stripping agent distributor; wherein the angle β between the direction of the gas outlet and the axial direction is 0 to 90°; the stripping agent is selected from liquid hydrocarbons and / or water.

[0072] The mixture of the vapor hydrocarbon mixture and the cooling aid is contacted with the gas stripping aid in countercurrent, and the gas phase material enters the cyclone separator 6 for preliminary separation treatment, so that the gas phase component enters the gas collecting chamber from the gas phase outlet of the cyclone separator 6; the obtained liquid phase component enters the tower plate 7 from the liquid phase outlet 3 of the cyclone separator 6 and the collecting pipe, is further processed through the tower plate 7, and the obtained liquid phase component is sent to the liquid storage space 10 below; the gas 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.

[0073] The present disclosure is further described in detail by way of examples. The raw materials used in the examples can be obtained through commercial sources. The final boiling point of the gas phase outlet product expected to be obtained in the following examples is 445°C.

[0074] Example 1

[0075] like Figure 1 As shown, a heavy hydrocarbon feedstock with an API value of 40 is used and the pressure is 0.4 MPa; Figure 3 As shown, the flash separation device comprises four baffles 9, and the angle between two adjacent baffles 9 is 90°, dividing the internal space of the vertical shell into four separation chambers of the same size. The stripping auxiliary agent is water vapor, and the cooling auxiliary agent is diesel.

[0076] After the heavy hydrocarbon raw material is heated to 270°C by the feed preheater, it is mixed with the primary steam heated by the dilution steam preheater to form a 280°C vapor hydrocarbon mixture; the vapor hydrocarbon mixture enters the feed and cooling aid mixing distributor through the vapor hydrocarbon mixture inlet 2 of the flash separation device, and the diesel at a temperature of 40°C enters the feed and cooling aid mixing distributor through the cooling / separation aid pipeline c. The vapor hydrocarbon mixture and the cooling aid are contacted in the feed and cooling aid mixing distributor and then enter the 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°; the weight ratio of diesel to vapor hydrocarbon mixture is 0.05:1.

[0077] 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 flash separation device through the stripping agent distributor; wherein the angle β between the direction of the gas outlet and the axial direction is 0°; and the weight ratio of water vapor as a stripping agent to the vapor hydrocarbon mixture is 0.05:1.

[0078] After the vapor-hydrocarbon mixture is contacted with water vapor and diesel in countercurrent, it enters the hydrocyclone 6 for preliminary separation treatment, so that the obtained gas phase component enters the gas collecting chamber through the gas phase outlet 1 of the hydrocyclone 6; the obtained liquid phase component enters the tower plate 7 through the liquid phase outlet 3 of the hydrocyclone 6 and the collecting pipe, is further processed through the tower plate 7, and the obtained liquid phase component is sent to the liquid storage space 10 below; the gas 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.

[0079] The properties of the gas phase and liquid phase components are shown in Table 1.

[0080] Example 2

[0081] like Figure 2 As shown, a heavy hydrocarbon feedstock with an API value of 40 is used and the pressure is 0.4 MPa; Figure 3 As shown, the flash separation device comprises four baffles 9, and the angle between two adjacent baffles 9 is 90°, dividing the internal space of the vertical shell into four separation chambers of the same size.

[0082] The heavy hydrocarbon feedstock is heated to 270°C by a feed preheater and then mixed with the primary dilution steam heated by a dilution steam preheater to form a 300°C vapor-hydrocarbon mixture; the vapor-hydrocarbon mixture enters the feed distributor through the vapor-hydrocarbon mixture inlet 2 of the flash separation device and then enters the separation device; wherein the angle η between the outlet of the feed distributor and the axial direction of the shell is 0°;

[0083] Diesel with a temperature of 40°C enters the cooling / separation aid inlet 4 of the separation device through the separation aid pipeline c and then enters the flash separation device through the separation aid distributor; wherein the angle γ between the direction of the air outlet and the axial direction is 0°; the weight ratio of the diesel as a separation aid to the gasoline hydrocarbon mixture is 0.05:1.

[0084] After the gaseous hydrocarbon mixture is contacted with water vapor and diesel in countercurrent, it enters the cyclone separator 6 for preliminary separation treatment, so that the obtained gas phase component enters the gas collecting chamber through the gas phase outlet 1 of the cyclone separator 6; the obtained liquid phase component enters the tower plate 7 through the liquid phase outlet 3 of the cyclone separator 6 and the collecting pipe, is further processed through the tower plate 7, and the obtained liquid phase component is sent to the liquid storage space 10 below; the gas 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.

[0085] The properties of the gas phase and liquid phase components are shown in Table 1.

[0086] Comparative Example 1

[0087] like Figure 3 As shown, the flash separation device used in this comparative example does not contain any components; a vapor-hydrocarbon mixture at a pressure of 0.4 MPa and a temperature of 280°C (the composition is the same as in Example 1) enters the flash separation device through the vapor-hydrocarbon mixture inlet 2 for gas-liquid separation, the gas phase rises and is discharged from the gas phase outlet 1 at the top of the tank, and the liquid is discharged from the liquid phase outlet 3 at the bottom of the tank.

[0088] The properties of the gas phase and liquid phase products are shown in Table 1.

[0089] Table 1 Properties of gas phase products and liquid phase products in Examples and Comparative Examples

[0090]

[0091]

[0092] As shown in Table 1, according to the comparison of the data in Examples 1 to 2 and Comparative Example 1, it can be seen that the flash separation equipment is isolated into a plurality of separation chambers arranged side by side by the baffle 9, and each separation chamber is provided with a vapor hydrocarbon mixture inlet 2 and a gas phase outlet 1, which can at least increase the system life by 50%. In addition, the components such as the cyclone separator 6, the feed distributor and the tray 7 are arranged in each separation chamber, which can improve the gas-liquid separation efficiency and the flash effect, so that the content of the heavy component at the top of the flash tank and the light component at the bottom of the flash tank are greatly reduced. In addition, by injecting one or more of the cooling aid, the separation aid or the gas stripping aid, the separation effect can be further improved, so that the heavy component at the top of the flash tank can be reduced to less than 0.20 weight%, the light component content at the bottom of the flash tank can be reduced to less than 10.9 weight%, and the decoking cycle can be extended by at least 50%.

[0093] The preferred embodiments of the present disclosure are described in detail above in conjunction with the accompanying drawings; however, the present disclosure is not limited to the specific details in the above embodiments. Within the technical concept of the present disclosure, a variety of simple modifications can be made to the technical solution of the present disclosure, and these simple modifications all fall within the protection scope of the present disclosure.

[0094] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. In order to avoid unnecessary repetition, the present disclosure will not further describe various possible combinations.

[0095] In addition, various embodiments of the present disclosure may be arbitrarily combined, and as long as they do not violate the concept of the present disclosure, they should also be regarded as the contents disclosed by the present disclosure.

Claims

1. A system for processing heavy hydrocarbons, characterized in that: The system includes a separation device; The separation device comprises a vertical shell, a tower tray arranged inside the vertical shell, a hydrocyclone separator arranged inside the vertical shell, a liquid storage space and an optional baffle; the hydrocyclone separator is arranged at the upper part of the vertical shell, the tower tray is arranged in the middle part of the vertical shell and below the hydrocyclone separator, and the liquid storage space is arranged at the lower part or outside of the vertical shell; the baffle is arranged vertically inside the vertical shell and the edge of the baffle is sealed and connected to the inner wall of the vertical shell, so as to divide the upper space in the vertical shell into a plurality of separation chambers arranged side by side; The separation device comprises a vapor-hydrocarbon mixture inlet, a cooling / separation aid inlet, a gas phase outlet, a liquid phase outlet and an optional gas stripping aid inlet; the vapor-hydrocarbon mixture inlet of the separation device is used to communicate with a heavy hydrocarbon source; the cooling / separation aid inlet of the separation device is used to communicate with a cooling aid source or a separation aid source; the gas stripping aid inlet of the separation device is used to communicate with a gas stripping aid source; the gas phase outlet of the separation device is used to communicate with a gas phase downstream device; and the liquid phase outlet of the separation device is used to communicate with a liquid phase downstream device.

2. The system according to claim 1, characterized in that The separation chamber comprises a hydrocyclone separator, a tower plate and a liquid storage space arranged in sequence from top to bottom; The hydrocyclone separator is arranged in the upper space of the separation chamber, so that the vapor-hydrocarbon mixture entering the separation chamber is flashed to obtain a gas phase component and a liquid phase component, and the gas phase component enters the hydrocyclone separator for separation to further separate the entrained liquid phase component; A cooling / separation aid storage or distributor is provided at the lower part of the inlet of the upper hydrocyclone 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 separation aid and enter the lower tray for further separation; The tower tray is arranged in the middle of the separation chamber and below the hydrocyclone separator, so that the liquid phase components separated by the hydrocyclone separator in the separation chamber can be further separated by the tower tray; The liquid storage space is arranged in the lower space of the separation chamber, so that the liquid phase components further separated by the tower plate in the separation chamber can flow into the liquid storage space.

3. The system according to claim 2, characterized in that The separation chamber is also provided with a sealing cover plate; the sealing cover plate is horizontally arranged above the hydrocyclone separator and the edge of the sealing cover plate is tightly combined with the side wall of the separation chamber, so that the upper space of the sealing cover plate forms a gas collecting chamber; The sealing cover plate is provided with a gas phase opening, and the gas phase opening is communicated with the gas phase outlet of the hydrocyclone separator, so that the gas phase separated by the hydrocyclone separator can enter the gas collecting chamber.

4. The system according to claim 3, characterized in that A collecting pipe is also provided in the separation chamber; the collecting pipe comprises a liquid phase inlet and a liquid phase outlet, the liquid phase inlet of the collecting pipe is connected with the liquid phase outlet of the hydrocyclone, and the liquid phase outlet of the collecting pipe extends to the inlet of the tower plate.

5. The system according to claim 4, characterized in that The number of stages of the hydrocyclone separator inside the separation chamber is more than 2.

6. The system according to claim 2, characterized in that A gas phase outlet is provided at the top of the separation chamber for communicating with a gas phase downstream device; A liquid phase outlet is provided at the bottom of the separation chamber for communicating with a liquid phase downstream device; A steam-hydrocarbon mixture inlet, a cooling / separation aid inlet and an optional gas stripping aid inlet are also provided on the side wall of the separation chamber; the steam-hydrocarbon mixture inlet of the separation chamber is used to communicate with a heavy hydrocarbon source; the cooling / separation aid inlet of the separation chamber is used to communicate with a cooling aid source or a separation aid source; the gas stripping aid inlet of the separation chamber is used to communicate with a gas stripping aid source.

7. The system according to claim 6, characterized in that The separation chamber also includes a feed and cooling agent mixing distributor and a stripping agent distributor; The two inlets of the feed and cooling aid mixing distributor extend to the outside of the separation chamber to form the steam-hydrocarbon mixture inlet and the cooling / separation aid inlet respectively; The inlet of the stripping agent distributor extends to the outside of the separation chamber to form the stripping agent inlet; the outlet of the feed and cooling agent 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 to 90°; 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 to 90°; or, The separation chamber also includes a separation aid distributor and a feed distributor; The inlet of the separation aid distributor extends to the outside of the separation chamber to form the cooling / separation aid inlet; the inlet of the feed distributor extends to the outside of the separation chamber to form the vapor-hydrocarbon mixture inlet; the outlet of the separation 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 to 90°; 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 to 90°.

8. The system according to claim 1, characterized in that The included angle between two adjacent baffles is 0 to 180 degrees.

9. The system according to claim 1, characterized in that The system also includes a feedstock line, a cooling / separation aid line, and an optional stripping aid line; The inlet of the raw material pipeline is connected to the heavy hydrocarbon source, and the outlet is connected to the vapor-hydrocarbon mixture inlet of the vertical shell; the inlet of the cooling / separation aid pipeline is connected to the cooling aid source or separation aid source, and the outlet is connected to the cooling / separation aid inlet of the vertical shell; the inlet of the stripping aid pipeline is connected to the stripping aid source, and the outlet is connected to the stripping aid inlet of the vertical shell; The raw material pipeline is provided with a feed preheater for heating the material in the raw material pipeline; the feed preheater is selected from one or more of a heating furnace, a cracking furnace convection section and a heat exchanger.

10. The system according to claim 9, characterized in that The system also includes a steam pipeline; the raw material pipeline is provided with a primary steam inlet and a secondary steam inlet; the stripping auxiliary agent pipeline is provided with a secondary steam inlet; The steam pipeline can be divided into a primary steam pipeline and a secondary steam pipeline; The inlets of the primary steam pipeline and the secondary steam pipeline are used to communicate with a steam source; the outlet of the primary steam pipeline is communicated with the primary steam inlet on the raw material pipeline; the outlet of the secondary steam pipeline is communicated with the secondary steam inlets on the raw material pipeline and the stripping agent pipeline; The primary steam pipeline and the secondary steam pipeline are provided with steam preheaters for heating steam; the steam preheaters are selected from one or more of a heating furnace, a cracking furnace convection section and a heat exchanger.

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