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WO2025036440A1 - Dispositif de séparation gaz-liquide et son utilisation dans la préparation d'oléfine par vapocraquage - Google Patents

Dispositif de séparation gaz-liquide et son utilisation dans la préparation d'oléfine par vapocraquage Download PDF

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Publication number
WO2025036440A1
WO2025036440A1 PCT/CN2024/112273 CN2024112273W WO2025036440A1 WO 2025036440 A1 WO2025036440 A1 WO 2025036440A1 CN 2024112273 W CN2024112273 W CN 2024112273W WO 2025036440 A1 WO2025036440 A1 WO 2025036440A1
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WO
WIPO (PCT)
Prior art keywords
gas
separation
liquid
liquid separation
inner cavity
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
PCT/CN2024/112273
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English (en)
Chinese (zh)
Inventor
王子宗
何细藕
吴德飞
林江峰
白飞
袁晴棠
刘敬坤
邵晨
赵永华
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China Petroleum and Chemical Corp
Sinopec Engineering Inc
Original Assignee
China Petroleum and Chemical Corp
Sinopec Engineering Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from CN202311041890.6A external-priority patent/CN119490865A/zh
Priority claimed from CN202322223564.9U external-priority patent/CN220758365U/zh
Application filed by China Petroleum and Chemical Corp, Sinopec Engineering Inc filed Critical China Petroleum and Chemical Corp
Publication of WO2025036440A1 publication Critical patent/WO2025036440A1/fr
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
    • B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
    • C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
    • C10G55/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step

Definitions

  • the present invention relates to the technical field of steam cracking, and more specifically to a gas-liquid separation device and its application in producing olefins by steam cracking.
  • 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.
  • CN03815733.0 discloses a steam cracking method for heavy hydrocarbon raw materials, wherein the raw materials are mixed with preheated heavy hydrocarbons, water and dilution steam to form a mixed stream, and then passed through a flash tank to separate the vapor phase from the liquid phase. The vapor phase is then passed through a separator to further The non-volatile matter is removed in the next step, and the gas phase product finally obtained enters the cracking furnace for cracking.
  • the object of the present invention is to provide a gas-liquid separation device and its application in steam cracking to produce olefins.
  • the gas-liquid separation device chamber division means fine control of individual adjustment of each chamber is achieved.
  • the purpose is to solve the problems in the prior art of the continuous enlargement of the scale of ethylene cracking furnaces, the increase in the number of feed groups, the continuous increase in feed amount, especially the violent production fluctuations caused by the presence of grouping and feeding different raw materials into the furnace chambers, resulting in low gas-liquid separation efficiency during operation, poor flash evaporation effect and difficulty in long-term operation.
  • the present invention relates to the following aspects.
  • the present invention relates to a method for producing olefins by steam cracking, comprising the following steps:
  • gas-liquid separation device for gas-liquid separation to obtain gas-phase material and liquid-phase material
  • an inner cavity which includes a top portion, an upper portion, a middle portion, a lower portion and a bottom portion
  • 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
  • the 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 the gas-liquid separation.
  • the present invention relates to 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
  • 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,
  • 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 integers from 1 to n.
  • the present invention relates to a gas-liquid separation method, comprising the step of transporting 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 described in any of the preceding or following aspects to perform gas-liquid separation.
  • a gas-liquid separation feed device preferably a gas-liquid separation feed distributor
  • the present invention uses a baffle to isolate the flash separation device into a plurality of separation chambers arranged side by side.
  • the high-temperature vapor-hydrocarbon mixture entering the separation chamber directly enters the downstream device from the gas phase outlet of the separation chamber after separation.
  • the operating parameters of each separation chamber are precisely controlled so that the fluctuation range of performance indicators such as the gasification rate of the separation chamber is less than 5%, and combined with the temperature control of the outlet of the furnace tube of the radiation section of the cracking furnace, the raw materials of the group are ensured to be in the best steam cracking state, thereby ensuring the stable operation of the cracking furnace to achieve the best product yield and a long coke cleaning cycle, further reducing the operation and maintenance costs and improving the economic benefits.
  • the present invention can reduce the content of heavy fractions and colloids and other impurities in the gas phase component by injecting cooling aids, washing aids and optional stripping aids, on the one hand, thereby improving the effect of gas-liquid separation, avoiding coking in the radiation section, thereby extending the coke cleaning cycle of the cracking furnace; on the other hand, it can reduce the content of light components in the liquid phase component.
  • injecting separation aids or stripping aids can strip out the light components in the liquid phase component to the maximum extent to obtain the 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 to improve the separation effect of the tower plate.
  • 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.
  • FIG. 1 is a schematic diagram of a heavy hydrocarbon steam cracking system according to the present invention (first embodiment series).
  • FIG. 2 is a schematic diagram of a heavy hydrocarbon steam cracking system according to the present invention (first embodiment series).
  • FIG3 is a front view of the gas-liquid separation device used in Comparative Example 1.
  • FIG. 4 is a top view of the gas-liquid separation device of the present invention (first embodiment series).
  • FIG. 5 is a schematic diagram of a gas-liquid separation device according to the present invention (second embodiment series).
  • FIG. 6 is a top view of the gas-liquid separation device of the present invention (second embodiment series).
  • FIG. 7 is a schematic diagram of a gas-liquid separation device in the prior art.
  • substantially means that deviations that are acceptable or reasonable to those skilled in the art are allowed to exist, such as deviations within ⁇ 2%, ⁇ 1%, ⁇ 0.5% or ⁇ 0.1%.
  • directional words such as “upper and lower” are generally used to 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” are relative to the outline of the device. More specifically, unless otherwise specified, directional words such as top, upper part, middle part, lower part and bottom part generally refer to the normal use state of the device.
  • 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 to the top head area
  • the middle generally refers to the area located near one-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 to the bottom head area
  • the upper part and the lower part generally refer to the area between the top and the middle part and the area between the middle and the bottom, respectively, but it is obvious to those skilled in the art that the present invention is not limited to this.
  • first, second are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated.
  • a feature defined as “first, second” may explicitly or implicitly include one or more of the feature.
  • the meaning of “plurality” is two or more, unless otherwise clearly and specifically defined.
  • primary dilution steam In the context of the present invention, the terms “primary dilution steam”, “secondary dilution steam” and the like are used only to distinguish the steam introduced in different steps, but do not contain any actual meaning such as the properties of the steam itself.
  • each device used in the present invention may use a structure conventionally selected in the art without any particular limitation.
  • heavy hydrocarbons refer to mixed hydrocarbons with a wide range, and their final boiling point is generally above 540°C, such as an initial boiling point temperature of 15°C and a final boiling point temperature of about 750°C.
  • the heavy hydrocarbons can be selected from one or more of the following raw materials: paraffin-based crude oil, intermediate-based crude oil, naphthenic crude oil, condensate oil and refined products.
  • refined products include gasoline, kerosene, diesel, tail oil, fuel oil, reformed oil, etc. that are processed by refineries through atmospheric and vacuum, reforming, catalytic, coking and other refining units.
  • the measurement method of the initial distillation point, the final distillation point and the distillation range is the 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.
  • API refers to specific gravity index
  • ASTM D-2320 ASTM D-2320
  • non-volatile components specifically refer to components with a final distillation point exceeding 590°C, and the analysis method for non-volatile components adopts ASTM D6352.
  • the gasification rate refers to the mass percentage of the gas phase material (excluding steam) to the total amount of feed (excluding steam).
  • a method for producing olefins by steam cracking is provided, in particular, a method for obtaining ethylene by steam cracking heavy hydrocarbons.
  • the present invention does not have specific and clear contents as follows, and those skilled in the art can directly apply the relevant information conventionally known in the art according to actual needs, and will not be repeated here.
  • a gas-liquid separation device comprising: an inner cavity, which includes a top, an upper part, a middle part, a lower part and a bottom, a liquid phase outlet, which is located at the bottom of the inner cavity, and a gas phase outlet, which is located at the top of the inner cavity.
  • the method for producing olefins by steam cracking and the gas-liquid separation device are combined together for specific description without distinguishing each other. Therefore, in the absence of special clarification, the content of the specific description of the method for producing olefins by steam cracking is also applicable to the gas-liquid separation device, and vice versa.
  • 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.
  • the method for producing olefins by steam cracking comprises step 1): heating heavy hydrocarbons to obtain a gas-liquid mixture.
  • step 1) the heavy hydrocarbon is heated to 100-400° C. (preferably 200-370° C.)
  • the heating can be carried out in any conventional manner known in the art without particular limitation, but is generally carried out in the convection section of the cracking furnace.
  • the final distillation temperature of the heavy hydrocarbon is above 540°C (preferably the initial distillation temperature is 15°C and the final distillation temperature is above 750°C).
  • the API value of the heavy hydrocarbon is not less than 32 (preferably above 38).
  • the heavy hydrocarbon is selected from at least one of paraffinic crude oil, intermediate crude oil, naphthenic crude oil, condensate oil and refined products.
  • the method for producing olefins by steam cracking comprises step 2): conveying the gas-liquid mixture into a gas-liquid separation device for gas-liquid separation.
  • 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.
  • the gas-liquid separation device further comprises one or more baffles, which 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 direction of the inner cavity.
  • each of the separation chambers comprises an upper portion, a middle portion and a lower portion.
  • n is an integer selected from 2-16 (preferably an integer selected from 4-8).
  • the inventors of the present invention have found that different numbers of separation chambers can be set according to the difference in the number of feed groups of the cracking furnace.
  • the number of separation chambers can be consistent with the number of feed groups, or it can be a multiple of the number of feed groups.
  • the performance indicators such as the gasification rate of the separation chamber can be accurately controlled so that the gasification rate fluctuation range is less than 5% (preferably less than 2%, more preferably less than 1% or less than 0.5%), ensuring that the group of raw materials In the best steam cracking state.
  • the operating temperatures of the gas-liquid separation are the same or different from each other, and are independently 100-400°C (preferably 200-370°C), and the operating pressures of the gas-liquid separation are the same or different from each other, and are independently 0.4-0.7MPaG.
  • the inventors of the present invention have found that according to the properties of the components entering the group of separation chambers, by independently adjusting the operating temperature or operating pressure of the separation chamber, the target gasification rate requirement is obtained, and the fluctuation range is below 5% (preferably below 2%, more preferably below 1% or below 0.5%), ensuring that the group of raw materials is in the best steam cracking state.
  • the gas-liquid separation device further comprises a gas-liquid separation feed device (preferably a gas-liquid separation feed 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.
  • a gas-liquid separation feed device preferably a gas-liquid separation feed distributor
  • the gas-liquid separation feed is sometimes also referred to as a vapor-hydrocarbon mixture.
  • the volumes of the n separation chambers are the same or different from each other, and may be evenly distributed among each other, or the volume of one or more separation chambers may be larger or smaller than that of other separation chambers, preferably, they are evenly distributed among each other.
  • 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.
  • a washing device preferably a washing aid distributor
  • a cooling device preferably a cooling aid distributor
  • a stripping device (preferably a stripping aid distributor) is arranged at the lower part and/or bottom of the inner cavity.
  • the gas-liquid separation component is a gas-liquid enhanced contact device.
  • any type of gas-liquid enhanced contact device conventionally known in the art can be used, such as a tray.
  • the column tray may be any type conventionally known in the art, and is not particularly limited.
  • the gas-liquid separation component is a centrifugal separation device.
  • the centrifugal separation device any type conventionally known in the art can be used, such as a cyclone separator.
  • the cyclone separator can be any type conventionally known in the art, without particular limitation.
  • the gas-liquid separation component is a filter device.
  • the filter device any type conventionally known in the art can be used, such as a demister, etc.
  • the demister can use any type conventionally known in the art, without particular limitation.
  • the gas-liquid separation component is a stripping device.
  • the stripping device any type conventionally known in the art can be used, and specifically, for example, a stripping agent distributor can be cited.
  • the stripping agent distributor can use any type conventionally known in the art, and there is no particular limitation.
  • the gas-liquid separation component is a washing device.
  • the washing device any type conventionally known in the art can be used, and specifically, for example, a washing aid distributor can be cited.
  • the washing aid distributor can use any type conventionally known in the art, and there is no particular limitation.
  • the gas-liquid separation component is a cooling device.
  • the cooling device any type conventionally known in the art can be used, and specifically, for example, a cooling aid distributor can be cited.
  • the cooling aid distributor can use any type conventionally known in the art, and there is no particular limitation.
  • the number of the gas-liquid separation components in each separation chamber can be reasonably set according to actual needs, but as an example, each can be independently selected from 0-20. In order to achieve a better technical effect of the present invention, it is preferred that the gas-liquid separation components of one or more separation chambers are set The number is different compared to other separation chambers, such as the difference is 1-4 or 1-2.
  • 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.
  • hydrocarbons such as light naphtha, naphtha, kerosene, light diesel, heavy diesel or hydrogenated tail oil
  • a partially condensed liquid phase preferably light diesel, condensate
  • the operating parameters of the cooling aid in different separation chambers may 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%.
  • 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).
  • hydrocarbons such as light naphtha, naphtha, kerosene, light diesel oil, heavy diesel oil or hydrogenated tail oil (preferably light diesel oil, condensate).
  • the operating parameters such as the temperature and flow rate of the washing aid, and those skilled in the art can reasonably choose according to actual conditions.
  • 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, such as a difference of more than 5%.
  • the stripping aid is selected from gaseous hydrocarbons and/or water vapor; water vapor can be steam such as low-pressure steam, dilution steam, medium-pressure steam and high-pressure steam; gaseous hydrocarbons can be at least one (preferably water vapor) of vaporized gas phases of hydrocarbons such as light naphtha, naphtha, kerosene or light diesel oil, or a mixture thereof.
  • water vapor can be steam such as low-pressure steam, dilution steam, medium-pressure steam and high-pressure steam
  • gaseous hydrocarbons can be at least one (preferably water vapor) of vaporized gas phases of hydrocarbons such as light naphtha, naphtha, kerosene or light diesel oil, or a mixture thereof.
  • the temperature of the mixture is generally not higher than 550°C, preferably 300-500°C, and more preferably 350-450°C.
  • the operating parameters of the stripping aid in different separation chambers may 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 a difference of more than 5%.
  • the gas-liquid separation feeding device and the gas-liquid separation The feed inlet is fluidly connected, 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.
  • 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 outlet and the central axis direction of the inner cavity is 0-90° (preferably 0°-30°).
  • 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 direction of the inner cavity is 0-90° (preferably 0°-30°).
  • the number of the gas-liquid separation feeding devices (preferably gas-liquid separation feeding distributors) disposed in each of the separation chambers is independently selected from 1-5 (preferably 1-2).
  • the number of the gas-liquid enhanced contact devices (preferably tower trays) disposed in each of the separation chambers is independently selected from 0-20 (preferably 5-15).
  • the number of the centrifugal separation devices (preferably cyclone separators) disposed in each of the separation chambers is independently selected from 0-20 (preferably 5-15).
  • the number of the filtering devices (preferably demisters) disposed in each of the separation chambers is independently selected from 0-3 (preferably 1-2).
  • the number of the stripping devices (preferably stripping aid distributors) disposed in each of the separation chambers is independently selected from 0-3 (preferably 1-2).
  • the number of the washing devices (preferably washing aid distributors) disposed in each of the separation chambers is independently selected from 0-3 (preferably 1-2).
  • the cooling device (preferably a cooling aid)
  • the number of distributors) disposed in each of the separation chambers is independently selected from 0-3 (preferably 1-2).
  • 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.
  • m and i are different and are independently selected from integers from 1 to n.
  • the inventors of the present invention have found that, especially in the case of group feeding or divided furnace feeding, when the feed composition is different, according to the properties of the group of raw materials, the number of gas-liquid separation components of the independent chambers can be flexibly set to further improve the gas-liquid separation effect of the group and ensure that the group of raw materials is in the best steam cracking state.
  • the gas-liquid separation component disposed inside the m-th separation chamber is different in number from the gas-liquid separation component disposed inside the i-th separation chamber (preferably, the difference in number is 1-4 or 1-2). Or, as an example, the gas-liquid separation component disposed inside the m-th separation chamber is different in type from the gas-liquid separation component disposed inside the i-th separation chamber.
  • the gas-liquid separation component disposed inside the m-th separation chamber and the gas-liquid separation component disposed inside the ith separation chamber both include a gas-liquid enhanced contact device (preferably a tower plate), but these devices differ in at least one indicator selected from the group consisting of the number of devices, separation efficiency, separation principle, operating parameters, device structure, and size specifications; 2) the gas-liquid separation component disposed inside the m-th separation chamber and the gas-liquid separation component disposed inside the ith separation chamber both include a centrifugal separation device ( Preferably, a cyclone separator), 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; 3) the gas-liquid separation component disposed inside the m-th separation chamber and the gas-liquid separation component disposed 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
  • the gas-liquid separation components arranged inside the m-th separation chamber and the gas-liquid separation components arranged inside the ith separation chamber all include a washing device (preferably a washing agent 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.
  • the gas-liquid separation components arranged inside the m-th separation chamber and the gas-liquid separation components arranged inside the ith separation chamber all include a cooling device (preferably a cooling agent 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.
  • a plurality of baffles are provided, and the angle between two adjacent baffles is 0-180° (preferably 30-90°).
  • 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.
  • the upper edge of at least one (for example, all) of the baffles is sealed and connected to the side wall of the top of the inner cavity.
  • the second gap there is a gap (called the 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.
  • the cyclone separator is arranged at the upper part of the separation chamber, and the tower plate is arranged below the cyclone separator (for example, arranged in the middle or lower part of the separation chamber).
  • the gas-liquid separation device is further provided with a collection
  • the manifold comprises a tube, wherein the liquid phase inlet of the manifold is fluidly connected to the liquid phase outlet of the cyclone separator, and the liquid phase outlet of the manifold is fluidly connected to the upper side of the tower tray.
  • a sealing cover plate is arranged on the top of the inner cavity in a horizontal direction, 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 arranged 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.
  • 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.
  • 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.
  • 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 that the liquid collected on the sealing cover plate can be transported to the internal space below the sealing cover plate (preferably to the liquid storage space) via the downcomer.
  • 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.
  • the cylindrical shell includes a top head, a cylinder of equal diameter and a bottom head from top to bottom.
  • the inner cavity diameter D of the cylinder of equal diameter is 3-10m
  • the inner cavity height H is 5-12m.
  • 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 inventor of the present invention has 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, further improving the separation effect of the gas-liquid separation device, and further reducing the fluctuation range of the gasification rate. Ensure that the group of raw materials is in the best steam cracking state.
  • the inner cavity diameter D1 of the large diameter cylinder is 3-10m
  • the inner cavity height H1 is 3-8m
  • the inner cavity diameter D2 of the small diameter cylinder is 1-5m
  • the inner cavity height H2 is 1-4m.
  • the lower edge of the baffle extends to the small diameter cylinder.
  • the cyclone separator is arranged at the upper part of the large diameter cylinder, and the tower plate is arranged at the upper part or the middle part of the small diameter cylinder.
  • the inventors of the present invention have found that after the gas phase component and the liquid phase component are initially separated by the cyclone separator, the liquid phase component entrained with the gas phase component in each cavity further increases the component concentration through the reduced diameter section, contacts with the arranged tower plate, further improves the heat transfer effect, thereby improving the separation effect of the gas-liquid separation device, and further reduces the fluctuation range of the gasification rate, ensuring that the group of raw materials is in the best steam cracking state.
  • the method for producing olefins by steam cracking further comprises step 3): combining at least two (such as all) of the n gas phase materials together to form a comprehensive gas phase material, and combining at least two (preferably all) of the n liquid phase materials together to form a comprehensive liquid phase material.
  • step 3) is an optional step, but preferably a necessary step.
  • the inventor of the present invention has found that combining at least two (for example, all) of the n gaseous materials to form a comprehensive gaseous material has obvious advantages in finely adjusting the gasification rate compared to not combining the n gaseous materials at all.
  • the average outlet temperature is usually used to control the heat load of the furnace by the cracking furnace.
  • the high-temperature vapor-hydrocarbon mixture enters the downstream device directly from the gas phase outlet of the above-mentioned separation chamber after separation, so that the fluctuation range of performance indicators such as the gasification rate of the separation chamber can be kept below 5%, and combined with the outlet temperature control of the radiation section furnace tube of the cracking furnace, it is ensured that the group of raw materials is in the best steam cracking state, thereby ensuring the stable operation of the cracking furnace to achieve the best product yield and a long coke cleaning cycle, further reducing the operating and maintenance costs and improving the economic benefits.
  • baffles to isolate the flash separation equipment into multiple separation chambers arranged side by side it also has obvious advantages in finely adjusting the gasification rate compared with the case where multiple tanks are arranged in parallel and the gas phase outlet materials are combined together.
  • it is difficult to achieve uniform distribution of the vapor-hydrocarbon mixture resulting in a large fluctuation range of performance indicators such as the vaporization rate before the gas-phase materials are combined.
  • the fluctuation range of performance indicators such as the vaporization rate will be significantly larger than that of the method of setting baffles to isolate the flash separation equipment into multiple separation chambers arranged side by side.
  • setting baffles to isolate the flash separation equipment into multiple separation chambers arranged side by side also has obvious advantages in reducing operating and maintenance costs and improving economic benefits.
  • the method for producing olefins by steam cracking comprises step 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 olefins.
  • the steam cracking can be carried out in any conventional manner known in the art, and the present invention is not particularly limited.
  • 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.
  • the performance index is selected from at least one of the gas phase final distillation point, the liquid phase final distillation point, the gas phase heavy component content, the liquid phase light component content, and the gasification rate.
  • 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.
  • the monitoring can be carried out in any conventional manner known in the art, and the present invention is not particularly limited.
  • a single-furnace cracking furnace as an example, during operation, there are controls on the total raw material hydrocarbon flow rate and the flow rate of each group of raw material hydrocarbons, balance and control of the cracking furnace outlet temperature, steam-to-hydrocarbon ratio control, and furnace heating control.
  • the feed of each group of cracking furnace coils is controlled by a flow control regulating valve.
  • the flow rate is measured by a flow meter.
  • flow meters provide accurate flow rates for each group of furnace tubes.
  • a total feed rate controller adjusts the set values of each group of feed controllers to control the amount of oil added to each furnace.
  • the amount of dilution steam mixed with each group of raw materials can be controlled by steam-to-hydrocarbon ratio control.
  • the degree can be used to determine whether the operation meets the requirements of the performance index range.
  • a thermocouple is set at the outlet of each group of furnace tubes in the cracking furnace, and the combustion load of each furnace is controlled by the average furnace outlet temperature.
  • the outlet temperature of each group of furnaces in the furnace is calculated to obtain the average furnace outlet temperature.
  • 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 aid pressure, cooling aid flow, and washing aid pressure, washing aid flow, etc., to ensure that the performance indicators are within the effective range, and the fluctuation range of performance indicators such as the gasification rate of the separation chamber is controlled to be below 5%.
  • 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 preceding or following aspects of the present invention to perform gas-liquid separation.
  • a gas-liquid separation feed device preferably a gas-liquid separation feed distributor
  • the gas-liquid separation device comprises a vertical shell, a tray 7 disposed inside the vertical shell, a cyclone separator 6 disposed inside the vertical shell, a liquid storage space 10 and an optional baffle 9;
  • the cyclone separator 6 is disposed at the upper part of the vertical shell, the tray 7 is disposed in the middle part of the vertical shell and below the cyclone separator 6, and the liquid storage space 10 is disposed at the lower part or outside of the vertical shell;
  • the baffle 9 is vertically disposed inside the vertical shell and the side of the baffle 9 is It 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/washing aid inlet 4, a gas phase outlet 1, a liquid phase outlet 3 and an optional stripping aid inlet 5;
  • the vapor-hydrocarbon mixture inlet 2 of the separation device is used to communicate with a heavy hydrocarbon source
  • the content of heavy fractions and impurities such as colloids in the gas phase component can be reduced, 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, the content of light components in the liquid phase component can be reduced.
  • injecting washing aids or stripping aids can strip out the light components in the liquid phase component to the maximum extent to obtain light components; 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.
  • the present invention 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 adjusting 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.
  • arranging 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, and avoid their coking in the radiation section, thereby further extending the decoking cycle of the cracking furnace.
  • 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.
  • the vertical shell is a conventional choice in the art, and the present invention can be reasonably selected according to different needs.
  • 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.
  • 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 component 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 component 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, 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/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.
  • 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.
  • 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.
  • the separation device is not provided with a stripping aid inlet 5.
  • the present invention also 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 steam-hydrocarbon mixture inlet 2 of the vertical shell, so that the steam-hydrocarbon mixture raw material can enter the separation device through the raw material pipeline a;
  • the cooling/washing aid pipeline c and an optional stripping aid pipeline d are connected;
  • the inlet of the raw material pipeline a is connected to the heavy hydrocarbon source, and the outlet is connected to the steam-hydrocarbon mixture inlet 2 of the vertical shell, so that the steam-hydrocarbon mixture raw material can enter the separation device through the raw material pipeline a;
  • the inlet of the 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
  • 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.
  • the present invention also 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 b
  • 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.
  • 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.
  • the steam entering the steam pipeline b includes one of dilution steam, low-pressure steam, medium-pressure steam or high-pressure steam.
  • the feed preheater can be flexibly controlled by adjusting the flow rate of the heating medium or the heater power in the feed preheater and the steam preheater. and the temperature of the primary steam and secondary steam preheaters, so that the phase state and temperature of the vapor-hydrocarbon mixture delivered to the gas-liquid separation device can be flexibly controlled, and the separation effect of the flash separation can be flexibly controlled.
  • one or more baffles 9 are arranged 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 0-180°, 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, and the angle between two adjacent baffles 9 is 90°, so that the internal space of the vertical housing is divided into four separation chambers of the same size.
  • 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.
  • 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.
  • 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.
  • the relative position relationship of the steam-hydrocarbon mixture inlet 2, the cooling/washing aid inlet 4 and the optional stripping aid inlet 5 is reasonably set.
  • the position relationship between the various inlets can be that the steam-hydrocarbon mixture inlet 2 and the cooling/washing aid inlet 4 are on the same horizontal line, and the stripping aid inlet 5 is arranged below; or the cooling/washing aid inlet 4, the steam-hydrocarbon mixture inlet 2 and the stripping aid inlet 5 are arranged in sequence from top to bottom; or the cooling/washing aid inlet 4, the steam-hydrocarbon mixture inlet 2 and the stripping aid inlet 5 are arranged in sequence from top to bottom; The cooling/washing aid inlet 4 and the steam hydrocarbon mixture inlet 2 are arranged in sequence from top to bottom.
  • 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 component.
  • the linking component 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 component.
  • the cooling/washing aid inlet 4 and the vapor-hydrocarbon mixture inlet 2 are both arranged below the inlet of the cyclone separator 6. In this embodiment, the problem that the vapor-hydrocarbon mixture, cooling aid and washing aid enter the cyclone separator 6 and affect the gas-liquid separation effect can be avoided.
  • the vapor-hydrocarbon mixture inlet 2 and the cooling/washing aid inlet 4 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 plate 7, and the separation chamber also includes a feed and cooling aid mixing distributor and a stripping aid distributor.
  • the two inlets of the feed and cooling aid mixing distributor respectively extend to the outside of the separation chamber 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 ⁇ between the direction of the outlet and the axial direction of the vertical shell is 0-90°.
  • 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 ⁇ between the direction of the outlet and the axial direction of the vertical shell is 0-90°.
  • the steam-hydrocarbon mixture and the cooling aid are respectively
  • the feed and cooling agent mixing distributor at both ends enter the feed and cooling agent mixing distributor and mix, which can make the vapor hydrocarbon mixture preliminarily condensed; the preliminarily condensed material enters the separation chamber through the outlet of the distributor.
  • the stripping medium distributor can make the stripping agent spray upward and fully contact with the preliminarily condensed material above, further enhancing the stripping effect, and further enhancing the gas-liquid separation effect and separation efficiency.
  • the separation chamber further includes a feed distributor and a washing aid distributor.
  • 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 ⁇ between the direction of the outlet and the axial direction of the vertical shell is 0-90°.
  • 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 ⁇ between the direction of the outlet and the axial direction of the vertical shell is 0-90°.
  • the feed distributor can 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 make the detergent flow downward, so that the detergent can be fully contacted 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.
  • the feed distributors, cooling aid distributors and stripping aid distributors in multiple separation chambers can be arranged at the same or different heights, depending on the temperature and pressure of the vapor hydrocarbon mixture.
  • the feed distributor, the feed and cooling aid mixing distributor, the washing aid distributor and the stripping aid distributor are provided with a plurality of opening areas as outlets of the distributor; the opening rate of the opening area is 5-15%, and the opening area is 20-30%.
  • the average pore size of the openings in the hole area is 10-20 mm.
  • 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.
  • the separation chamber comprises a cyclone separator 6, a tower tray 7 and a liquid storage space 10 which are arranged in sequence from top to bottom.
  • 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 gas phase components and liquid phase components through the cyclone separator 6;
  • the tower plate 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 by 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.
  • the liquid storage space 10 can be independently disposed outside the separation chamber.
  • the tower tray 7 and the cyclone separator 6 are conventionally selected in the art, and the present invention does not make special requirements.
  • 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.
  • 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.
  • the cyclone separator inside the separation chamber The number of stages of 6 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 separation device can enter the liquid collection area below through the manifold.
  • 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 separation devices can enter the tower plate 7 below through the manifold.
  • 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 plate below for further separation.
  • 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 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 cyclone separator 6, so that the gas phase separated by the cyclone separator 6 can enter the gas collecting chamber.
  • the gas phase components in the separation chamber can be discharged from the separation device only through the gas phase outlet 1 of the cyclone separator 6, further improving the effect of gas-liquid separation.
  • a method for treating heavy hydrocarbons using the system of the present invention comprises:
  • the heavy hydrocarbon feedstock is mixed with the primary dilution steam heated by the dilution steam preheater after passing through the feed preheater to form a vapor-hydrocarbon mixture of 100-400°C (preferably 200-370°C);
  • the vapor-hydrocarbon mixture enters the feed and cooling aid mixing distributor through the vapor-hydrocarbon mixture inlet 2 of the gas-liquid separation device;
  • the cooling aid enters the other end of the feed and cooling aid mixing distributor through the cooling/washing aid pipeline c;
  • the cooling aid enters the separation device after contacting the feed and the cooling aid mixing distributor; wherein the angle ⁇ between the outlet of the feed and the cooling aid mixing distributor and the axial direction of the shell is 0-90°;
  • the cooling aid is selected from liquid hydrocarbons and/or water.
  • 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 ⁇ 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.
  • a mixture of a vapor hydrocarbon mixture and a cooling aid is contacted with a stripping aid in countercurrent, and the gaseous material enters a cyclone separator 6 for preliminary separation treatment, so that the gaseous 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.
  • the gas-liquid separation device at least includes a vertical shell 1, a cyclone separator group 5 arranged inside the vertical shell 1, a tower plate 3 arranged inside the vertical shell 1, a liquid collection area 9 and an optional baffle 10.
  • 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 collecting area 9 is arranged below the tower tray 3.
  • the baffle 10 is vertically arranged inside the vertical shell 1, and the upper edge of the baffle 10 is sealed and 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; the lower edge of the baffle 10 has a gap with 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, each of the separation chambers is respectively connected to the liquid collection area 9, and the bottom of the liquid collection area 9 is provided with a liquid phase outlet 16;
  • 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 agent inlet 14.
  • the inlet steam distributor 4, the first flow guide distribution module and the second flow guide distribution module are used to evenly distribute the reaction materials entering the gas-liquid separation device, which can effectively avoid the problem of poor flash deliquescence effect due to uneven feed concentration.
  • the cyclone separator group 5 by using the cyclone separator group 5, the shear stress of the cyclone field of the cyclone separator and the sedimentation effect of the spatial gravity field 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 gas phase entrained droplets.
  • the vertical shell 1 is isolated into a plurality of separation chambers arranged side by side by a baffle 10.
  • 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 after separation. 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 temperature, and thus, can improve the life of the system.
  • the vertical shell 1 is a conventional choice in the art and can be reasonably selected according to different needs.
  • 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.
  • the lower edge of the baffle 10 extends to the lower part of the small-diameter cylinder.
  • the second necking section and a portion of the lower portion of the small-diameter cylinder form a liquid collecting area 9.
  • the cyclone separator group 5 is arranged on the upper part of the large-diameter cylinder.
  • the tower tray 3 is arranged on the upper part of the small-diameter cylinder.
  • 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.
  • the cooling/washing aid inlet 13 and the steam-hydrocarbon mixture inlet 12 are both arranged on the side wall of the large diameter cylinder of the vertical shell; the stripping aid inlet 14 is arranged on the side wall of the small diameter cylinder of the vertical shell.
  • the positional relationship between the cooling/washing aid inlet 13 and the steam-hydrocarbon mixture inlet 12 needs to be determined according to actual work requirements.
  • the cooling/washing aid inlet 13 and the steam-hydrocarbon mixture inlet 12 can be on the same horizontal line, or the cooling/washing aid inlet 13 can be below the steam-hydrocarbon mixture inlet 12.
  • the inlet steam distributor 4 when the cooling/washing aid inlet 13 is below the steam-hydrocarbon mixture inlet 12, the inlet steam distributor 4 is arranged above the first diversion distribution module, and some distance is left between the two.
  • the cooling/washing aid inlet 13 and the steam-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
  • the inlet steam distributor 4 and the first diversion distribution module are connected through a linking component.
  • the linking component is conventionally selected in the art so that the materials entering through the steam-hydrocarbon mixture inlet 12 and the cooling/washing aid inlet 13 can be evenly mixed in the linking component.
  • the cooling/washing aid inlet 13 of the gas-liquid separation device is used to communicate with the cooling/washing aid source through a pipeline;
  • the steam-hydrocarbon mixture inlet 12 is used to communicate with the steam-hydrocarbon mixture source through a pipeline;
  • the stripping aid inlet 14 is used to communicate with the stripping aid source through a pipeline.
  • the cooling aid and washing aid used in the cooling/washing aid source and the stripping aid used in the stripping aid source can be independently selected from liquid hydrocarbons and/or water vapor;
  • the water vapor can be low-pressure steam, medium-pressure steam, high-pressure steam, etc.;
  • the liquid hydrocarbon can be light naphtha, petroleum ether, etc. Hydrocarbons such as naphtha, kerosene, light diesel, heavy diesel or hydrogenated tail oil.
  • the baffles 10 can be selected conventionally in the art, and the present invention does not make special requirements.
  • the number of two adjacent baffles 10 can be 0, 1, 2, 3, 4 or more than 4, preferably less than 4.
  • the angle between two adjacent baffles 10 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°.
  • the cyclone separator group 5 is mainly composed of one or more cyclone separators, preferably the number of cyclone separators in the cyclone separator group 5 is 2 or more, more preferably 6.
  • n cyclone separators are connected in series to form an n-stage cyclone separator group, for example, a three-stage cyclone separator is formed by three cyclone separators connected in series.
  • the cyclone separator group 5 is composed of two groups of three-stage cyclone separators.
  • 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.
  • a 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.
  • the lengths of the material legs of the three-stage cyclone separators may be the same or different.
  • the length of the material legs of the first-stage cyclone separator is greater than the length of the material legs of the second-stage cyclone separator
  • the length of the material legs of the second-stage cyclone separator is greater than the length of the material legs of the third-stage cyclone separator.
  • the separation chamber is further provided with a horizontal partition
  • the horizontal partition plate 7 is horizontally arranged 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.
  • 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 collecting chamber 8.
  • 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.
  • 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 collecting area 9, so that the liquid phase separated by the cyclone separator group 5 can enter the liquid collecting area 9 through the manifold 11.
  • 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.
  • the included angle of the V-shaped tubular shape may be consistent with the included angle between the necking section and the small diameter cylinder.
  • a fixing piece is further provided in the separation chamber for fixing the manifold 11 inside the vertical housing 1 .
  • the tower tray 3 is conventionally selected in the art, and the present invention does not make any special requirements.
  • the lower surface of the inlet steam distributor 4, the lower surface of the first flow diversion distribution module and the upper surface of the second flow diversion distribution module in the separation chamber are all provided with a plurality of opening areas as material nozzles; the porosity of the opening areas is 5-15%, and the average pore size of the openings in the opening areas is 10-20 mm.
  • the angle ⁇ 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°.
  • a material nozzle is provided on the lower surface of the first flow diversion distribution module; an angle ⁇ 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°.
  • an angle ⁇ 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°.
  • the first flow guide distribution module is arranged below the inlet of the cyclone separator group 5 ; the second flow guide distribution module is arranged below the inlet of the tower tray 3 .
  • 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 can be discharged from the device through the gas phase outlet 15 .
  • the steam-hydrocarbon mixture is evenly mixed in the separation chamber through the first flow diversion distribution module, the washing aid or cooling medium is evenly mixed through the inlet steam distributor 4, and the stripping aid is evenly mixed through the second flow diversion distribution module, which can enhance the stripping effect and further enhance the gas-liquid separation effect and separation efficiency.
  • the method for producing olefins by steam cracking of the present invention comprises: allowing a heavy hydrocarbon feedstock heated to 100-400° C. (preferably 200-370° C.) to enter a separation chamber through a first flow distribution module; allowing a cooling agent to enter the separation chamber through an inlet steam distributor 4; allowing a stripping agent to enter the separation chamber through a second flow distribution module; allowing a mixture of a steam-hydrocarbon mixture and a cooling agent to contact the stripping agent in countercurrent, and allowing the gas phase material to enter a cyclone separator group 5 for preliminary separation.
  • the gas phase components are separated and treated 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 products in the overflow collection chamber 8 are discharged through the gas phase outlet 15, and the liquid phase products in the liquid collection area 9 are discharged through the liquid phase outlet 16.
  • the raw materials used in the examples and comparative examples were all obtained from commercial sources.
  • 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 about 445° C., and the control index value taking time is 6 hours.
  • a heavy hydrocarbon raw material with an API value of 40 is used; as shown in Figure 1, the gas-liquid separation device is composed of 4 baffles 9, and the angle between two adjacent baffles 9 is 90°, which divides the internal space of the vertical shell into 4 separation chambers of the same size.
  • the operating temperature of each separation chamber is 280°C and the operating pressure is 0.4MPaG.
  • the stripping aid is water vapor and the cooling aid is diesel.
  • each internal space is configured in the same way, and a cooling aid distributor, a stripping aid distributor, a defoamer, 5 trays, and 5 secondary cyclone separators are set.
  • the cooling agent distributor is provided with 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 is provided with 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 a top-mounted type;
  • the tower plate is a block type; and the secondary cyclone separator is an integrated type.
  • 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 by the feed preheater, each group is mixed with the primary steam heated by the 22,400 kg/h dilution steam preheater through steam-hydrocarbon ratio control to form a 280°C steam.
  • the vapor hydrocarbon mixture enters the feed and cooling aid mixing distributor through the vapor hydrocarbon mixture inlet 2 of the gas-liquid separation device, and the diesel at a temperature of 40°C enters the feed and cooling aid mixing distributor through the cooling/washing 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 ⁇ between the direction of 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 the vapor hydrocarbon mixture is 0.05:1.
  • 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 ⁇ between the direction of the gas outlet and the axial direction is 0°; the weight ratio of water vapor as a stripping agent to the gas-hydrocarbon mixture is 0.05:1.
  • the gas-hydrocarbon mixture After the gas-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 from the gas phase outlet 1 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 four groups are combined and sent to the cracking furnace for further processing, and 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.
  • the average furnace outlet temperature of the device is set at 820°C. Under this balance and control of the cracking furnace outlet temperature, 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.
  • Example 2 The same as Example 1, except that one of the chambers is not provided with a cooling aid distributor and a stripping aid distributor.
  • Example 2 The same as Example 1, except that one of the chambers is not provided with a demister and a tray.
  • Example 2 The same as Example 1, except that the number of trays in one chamber is set to 15.
  • Example 2 The same as Example 1, except that the number of cyclone separators in one chamber is set to 15.
  • one of the chamber cyclone separators is a three-stage cyclone separator.
  • Example 2 The same as Example 1, except that the diameter of the tray arranged in one of the chambers is increased by 20%.
  • Example 2 Same as Example 1, except that the cyclone separators arranged in one chamber are The volume increased by 20%.
  • Example 2 The same as Example 1, except that the diesel consumption in one chamber is increased by 10%.
  • Example 2 The same as Example 1, except that the diesel temperature in one chamber is adjusted to 60°C.
  • Example 2 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.
  • Example 2 The same as Example 1, except that the shell gas phase outlet is connected to the downstream device as a single furnace cracking furnace convection section, and the cracking furnace has two groups of raw material feed and two groups of cross-tubes. Every two inner cavity outlets of the shell are combined into one gas phase outlet, a total of two gas phase outlets 1, and the heavy hydrocarbon feedstock and dilution steam are evenly distributed accordingly.
  • the cracking furnace convection section has four groups of raw material feed and four groups of cross-tubes, three of which feed heavy hydrocarbon raw materials with an API value of 40, and the other group feeds conventional naphtha raw materials.
  • the three inner cavity outlets for feeding heavy hydrocarbon raw materials are combined into one gas phase outlet, and the inner cavity for feeding conventional naphtha raw materials is a separate gas phase outlet, with a total of two gas phase outlets1.
  • 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 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 manner, wherein each cavity of the large diameter cylinder is provided with a cooling aid distributor, a defoamer, and 5 secondary cyclone separators, and each cavity of the small diameter cylinder is provided with a stripping aid distributor and 5 tower plates.
  • the rest is the same as in Example 1.
  • Example 12 The same as Example 12, except that the tower plate arranged in the small diameter cylinder is moved to the lower part of the large diameter cylinder.
  • FIG. 3 it is the same as Example 1, except that no baffle is provided in the gas-liquid separation device.
  • Example 2 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 trays are the same as those of a single chamber configuration, and no baffle is set.
  • the flash separation equipment is isolated into a plurality of separation chambers arranged side by side by the baffle 9, and by increasing the number of cyclone separators or trays in a separate chamber, changing the size of the cyclone separators or trays, using different cyclone separators or tray types, changing the flow rate and temperature of the stripping aid or cooling aid, or setting a reduced diameter section, the operation of each chamber can be finely controlled, the fluctuation of the outlet gasification rate is effectively reduced, and the fluctuation of the feed amount entering the radiation section furnace tube is controlled to ensure the smooth operation of the cracking furnace.
  • the variation range of the operating parameters of the gas-liquid separator can be reduced to a minimum of about 0.5%, and all embodiments can increase the system life by at least 50% compared with the comparative example.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

La présente invention concerne un dispositif de séparation gaz-liquide et son utilisation dans la préparation d'oléfine par vapocraquage. Un procédé de préparation d'oléfine par vapocraquage de la présente invention comprend les étapes suivantes : le chauffage d'hydrocarbures lourds pour obtenir un mélange gaz-liquide ; le transport du mélange gaz-liquide dans un dispositif de séparation gaz-liquide pour la séparation gaz-liquide de manière à obtenir des matériaux en phase gazeuse et des matériaux en phase liquide, ledit dispositif de séparation gaz-liquide présentant une cavité interne, une sortie en phase liquide, une sortie en phase gazeuse, un ou plusieurs déflecteurs, qui divisent au moins le milieu de la cavité interne en n chambres de séparation dans la direction de l'axe central de la cavité interne, un dispositif d'alimentation de séparation gaz-liquide, et des composants de séparation gaz-liquide, qui sont respectivement agencés à l'intérieur des n chambres de séparation et sont conçus pour pouvoir effectuer respectivement une séparation gaz-liquide dans les n chambres de séparation, de manière à obtenir les n matériaux en phase gazeuse correspondants et n matériaux en phase liquide ; et la réalisation d'un vapocraquage sur au moins l'un des n matériaux en phase gazeuse ou des matériaux en phase gazeuse combinés pour obtenir un produit de craquage contenant de l'oléfine. Le dispositif de séparation gaz-liquide de la présente invention présente les caractéristiques d'un fonctionnement à longue période, etc.
PCT/CN2024/112273 2023-08-17 2024-08-15 Dispositif de séparation gaz-liquide et son utilisation dans la préparation d'oléfine par vapocraquage Pending WO2025036440A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
CN202311041890.6 2023-08-17
CN202311041890.6A CN119490865A (zh) 2023-08-17 2023-08-17 一种处理重质烃的系统
CN202322223564.9 2023-08-17
CN202322223564.9U CN220758365U (zh) 2023-08-17 2023-08-17 一种用于蒸汽裂解装置蒸汽的脱液装置

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001054785A2 (fr) * 2000-01-24 2001-08-02 Basf Aktiengesellschaft Colonne compartimentee
CN101796167A (zh) * 2007-08-21 2010-08-04 埃克森美孚化学专利公司 烃原料的蒸汽裂化方法和设备
CN102380262A (zh) * 2010-09-01 2012-03-21 中国石油化工股份有限公司 一种高压分离器及高压分离的方法
CN110387253A (zh) * 2018-04-19 2019-10-29 中国石油大学(华东) 一种两段提升管催化裂化防结焦沉降器
CN210645178U (zh) * 2019-09-07 2020-06-02 广东香龙香料有限公司 用于香精提取的水蒸气蒸馏装置
CN220758365U (zh) * 2023-08-17 2024-04-12 中国石油化工股份有限公司 一种用于蒸汽裂解装置蒸汽的脱液装置

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001054785A2 (fr) * 2000-01-24 2001-08-02 Basf Aktiengesellschaft Colonne compartimentee
CN101796167A (zh) * 2007-08-21 2010-08-04 埃克森美孚化学专利公司 烃原料的蒸汽裂化方法和设备
CN102380262A (zh) * 2010-09-01 2012-03-21 中国石油化工股份有限公司 一种高压分离器及高压分离的方法
CN110387253A (zh) * 2018-04-19 2019-10-29 中国石油大学(华东) 一种两段提升管催化裂化防结焦沉降器
CN210645178U (zh) * 2019-09-07 2020-06-02 广东香龙香料有限公司 用于香精提取的水蒸气蒸馏装置
CN220758365U (zh) * 2023-08-17 2024-04-12 中国石油化工股份有限公司 一种用于蒸汽裂解装置蒸汽的脱液装置

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