WO2022166751A1 - 分馏塔 - Google Patents

分馏塔 Download PDF

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Publication number
WO2022166751A1
WO2022166751A1 PCT/CN2022/074297 CN2022074297W WO2022166751A1 WO 2022166751 A1 WO2022166751 A1 WO 2022166751A1 CN 2022074297 W CN2022074297 W CN 2022074297W WO 2022166751 A1 WO2022166751 A1 WO 2022166751A1
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Prior art keywords
section
pipeline
gas
fractionation column
fractionation
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PCT/CN2022/074297
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English (en)
French (fr)
Inventor
王振维
赵百仁
赵明瑞
杨丽庆
刘罡
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China Petroleum and Chemical Corp
Sinopec Engineering Inc
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China Petroleum and Chemical Corp
Sinopec Engineering Inc
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Publication of WO2022166751A1 publication Critical patent/WO2022166751A1/zh
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G7/00—Distillation of hydrocarbon oils
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C11/00—Aliphatic unsaturated hydrocarbons
    • C07C11/02—Alkenes
    • C07C11/04—Ethene
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
    • C07C4/04—Thermal processes
    • 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
    • C10G7/00—Distillation of hydrocarbon oils
    • C10G7/12—Controlling or regulating
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline

Definitions

  • the present invention relates to the field of ethylene production, more particularly to a fractionation column and its use in a steam cracking ethylene plant.
  • the liquid raw material cracking gas recovers heat through the waste boiler, and after being cooled by the quenching oil sprayed by the quencher, it is mixed with the gaseous raw material cracking gas whose heat is recovered by the waste boiler, and enters the quenching oil section at the lower part of the gasoline fractionation tower.
  • the gaseous raw material pyrolysis gas gas phase, temperature about 200 °C
  • the liquid raw material pyrolysis gas recovers heat through the waste boiler, and is cooled by the quencher spraying and cooling the quench oil.
  • the temperature is about 400 °C
  • the content of coke particles and heavy components is large
  • the physical properties of the two streams are very different
  • the mixing treatment is uneconomical
  • the separation load is artificially increased.
  • the quenching oil section of the gasoline fractionation tower of the traditional ethylene plant is equipped with a herringbone baffle or an angle steel to remove the coke particles in the cracked gas.
  • the quenching oil is extracted from the bottom of the quenching oil section of the gasoline fractionation tower, carrying a large amount of heavy components and coke particles.
  • a pre-pump filter In order to remove the coke particles in the quenching oil, a pre-pump filter must be installed before the quenching oil circulating pump, and a hydrocyclone and a static device should be installed after the quenching oil circulating pump.
  • the equipment investment is high, and the number of equipment is large, which increases the occupation land area.
  • the traditional ethylene plant needs a separate viscosity reducing tower.
  • high temperature gas raw material cracking gas temperature 450-505°C
  • high pressure steam as stripping medium
  • a part of quench oil is introduced into the viscosity reducing tower for stripping
  • the heavy components are extracted from the tower kettle of the viscosity reducing tower, and the required middle distillate is returned to gasoline Fractionation tower.
  • the operating temperature of the viscosity reducing tower is usually around 250-280°C.
  • the heat of the pyrolysis gas of the high-temperature gas feedstock is transferred to the quench oil with only 180-200°C, and the heat utilization is not economical enough. And in actual operation, because the heavy components are very easy to block the tower kettle of the viscosity reduction tower at high temperature, the operating temperature of the viscosity reduction tower is much lower than the design value, and the viscosity reduction effect is poor. If the quench water is forced to decrease, the heat taken by the gasoline fractionation tower tower will decrease, the heat will move up, and the temperature at the top of the tower will increase, which will easily cause emulsification of the quench water in the downstream quench water tower and affect the stable operation of the ethylene unit.
  • the quench oil is used as a heat source to generate dilution steam, the temperature of the quench oil drops, and the amount of dilution steam is reduced, which requires more consumption of medium-pressure steam to generate dilution steam, resulting in an increase in energy consumption of the ethylene plant.
  • the present invention provides a novel gasoline fractionation tower for an ethylene plant.
  • the gasoline fractionation tower can achieve better coke particle removal and quench oil viscosity reduction, which is beneficial to the long-term stable operation of the ethylene plant and energy saving and consumption reduction.
  • a first aspect of the present invention provides a fractionation column, the fractionation column comprises a shell and a partition plate arranged in the shell, and the partition plate divides the inside of the shell into a lower section A and an upper section B
  • the side wall of the lower section A is provided with at least two openings, which are respectively communicated with the gas pipeline and the mixed-phase pipeline; the bottom of the lower section A is communicated with the fuel oil extraction pipeline; the bottom of the upper section B is provided with a quenching oil extraction outlet, The quenching oil extraction outlet is communicated with the quenching oil extraction pipeline; a number of openings are arranged on the baffle plate, which are respectively connected with a number of air risers, so that the lower A section and the upper B section are communicated.
  • a second aspect of the present invention provides the use of a fractionation column in a steam cracking ethylene plant.
  • the fractionation tower of the invention can realize better coke particle removal and quench oil viscosity reduction, which is beneficial to long-term stable operation of the ethylene plant and energy saving and consumption reduction.
  • the fractionation column has the following advantages:
  • the tower has a compact structure, which integrates the viscosity reduction tower of the traditional ethylene plant and the gasoline fractionation tower.
  • the high-grade heat source of the high-temperature gas raw material cracking gas can be used to generate steam and reduce the energy consumption of the device.
  • FIG. 1 is a schematic structural diagram of the first embodiment of the fractionation column of the present invention.
  • FIG. 2 is a cross-sectional view of the plane A-A in FIG. 1 .
  • Fig. 3 is a schematic structural diagram of the second embodiment of the fractionation column of the present invention.
  • FIG. 4 is a cross-sectional view of the plane A-A in FIG. 3 .
  • FIG. 5 is a schematic structural diagram of a third embodiment of the fractionation column of the present invention.
  • FIG. 6 is a cross-sectional view of the plane A-A in FIG. 5 .
  • the fractionation tower of the present invention comprises a shell and a partition plate arranged in the shell, the partition plate divides the inside of the shell into a lower A section 1 and an upper B section 2, and a coke cleaning facility is arranged in the lower A section 1; the lower A section 1
  • the side wall is provided with at least two openings, which are respectively connected with the gas pipeline 6 and the mixed phase pipeline 7; the bottom of the lower A section 1 is provided with a liquid collecting bag 10, and the bottom of the liquid collecting bag 10 is communicated with the fuel oil extraction pipeline 11; the bottom of the upper B section 2 is provided with The quenching oil extraction outlet 8, the quenching oil extraction outlet 8 is communicated with the quenching oil extraction pipeline 13; a number of openings are provided on the clapboard, and a number of air risers 9 are connected respectively, so that the lower A section 1 and the upper B section 2 are communicated;
  • the cracked gas inner extension pipe 5 is communicated with the gas pipeline 6; the top of the coke cleaning facility is provided with a rising pipe
  • the coke cleaning facility may be at least one of a coke cleaning tank, a single cyclone, and a combination of multiple cyclones. When a combination of multiple cyclones is used, the combination can be arranged in the coke cleaning tank.
  • the cracked gas inner extension pipe 5 can be tangentially connected to the coke cleaning facility.
  • the upper B section 2 can be provided with internals, and the internals are preferably trays, packings or combinations thereof; the upper B section 2 can be divided into 2-4 small sections, preferably quenching oil section, pan oil section and refining section from bottom to top. Distillation section.
  • the riser 9 can be arranged in the upper B section 2, and the height of its outlet end can reach above the high liquid level of the quench oil; the riser 4 in the upper B section 2 can reach above the high liquid level of the quench oil.
  • the bottom structure of the upper B section 2 can be a head or a sump.
  • Vortex breakers 15 and 16 may be provided at the bottom of the upper B section 2 and the bottom of the liquid collecting bag 10, respectively.
  • the side wall opening of the lower A section 1 communicating with the gas line 6 may not be higher than the side wall opening of the lower A section 1 communicating with the miscible phase line 7 .
  • the fractionation tower of the present invention is preferably used in a steam cracking ethylene plant with both liquid raw materials and gaseous raw materials, wherein the gas pipeline 6 is a pipeline for transporting the gaseous raw material cracked gas, and the miscible phase pipeline 7 is a pipeline for transporting the liquid raw material cracked gas and quenching oil .
  • the liquid feedstock can be selected from one or more of C5 and above light hydrocarbons, naphtha, diesel oil and hydrogenation tail oil;
  • the gas feedstock can be selected from ethane, propane, butane, refinery dry gas and LPG one or more of.
  • the fractionation column used in Example 1 includes a shell and a partition plate arranged in the shell, and the partition plate divides the interior of the shell into a lower flash section 1 (ie, a lower section A) and an upper fractionation section Section 2 (ie, upper section B), flash section 1 is provided with a cyclone 3 .
  • the two openings on the side wall of the flash section 1 are respectively communicated with the gas line 6 and the miscible line 7 (the side wall opening of the flash section 1 communicating with the gas line 6 is lower than the side wall opening of the flash section 1 communicating with the miscible line 7) .
  • a liquid collecting bag 10 is arranged at the bottom of the flashing section 1, a second vortex breaker 16 is arranged at the bottom of the liquid collecting bag 10, and the bottom opening of the liquid collecting bag 10 is communicated with the fuel oil extraction line 11.
  • the cyclone separator 3 is communicated with the gas pipeline 6 through the inner extension pipe 5 of the cracked gas, the rising pipe 4 at the top of the cyclone separator 3 is inserted into the fractionation section 2, until the high liquid level of the quenching oil is above, and the coke particle discharge pipe 12 at the bottom of the cyclone separator 3 is downward. It extends to the bottom head of the tower and communicates with the external coke discharge line 14 .
  • a number of openings are provided on the clapboard, which are respectively connected with a number of gas risers 9, and a number of gas risers 9 are arranged in the fractionation section 2, and the height of its outlet end reaches the high liquid level of the quenching oil.
  • the extraction port 8 is communicated with the quench oil extraction pipeline 13, and the first vortex breaker 15 is arranged at the bottom.
  • the flashing section 1 is not provided with fractionation internals
  • the fractional fractionation section 2 is provided with quenching oil section, pan oil section and rectifying section from bottom to top, and is provided with tray internals.
  • the gas pipeline 6 and the miscible pipeline 7 are distributed at 90°, the outer end of the cracked gas inner extension pipe 5 is communicated with the gas pipeline 6, the inner end is tangentially connected with the cyclone separator 3, and the bottom of the fractionation section 2 is provided with 5 liters
  • the gas pipe 9 and the rising pipe 4 at the top of the cyclone separator 3 together form 6 openings distributed at 60° intervals.
  • the inner diameter of the fractionation tower is 13000mm
  • the diameter of the gas pipeline 6 is 2000mm
  • the diameter of the mixed phase pipeline 7 is 2600mm
  • the inner diameter of the liquid collecting bag 10 is 1200mm
  • the diameter of the riser 4 is 2000mm
  • the diameter of the gas riser 9 is 2500mm
  • the diameter of the quench oil extraction outlet is 1400mm.
  • the diameter of the cyclone separator 3 is 4500 mm
  • the diameter of the coke particle discharge pipe 12 is 100 mm.
  • the heat is recovered through the waste pot, and the liquid raw material pyrolysis gas cooled by the quench oil is sprayed by the quench cooler, and the temperature is about 250-280 ° C.
  • Gas-liquid separation the obtained gas phase enters the fractionation section 2 through the gas riser 9 at the bottom of the fractionation section 2, the obtained coke particles and liquid phase heavy components are accumulated at the bottom of the flash section 1, and are discharged through the fuel oil extraction line 11 at the bottom of the liquid collection bag 10;
  • the pyrolysis gas at the outlet of the gas furnace where the heat is recovered from the boiler, at about 200 °C enters the flashing section 1 of the fractionation tower through the gas pipeline 6, and enters the cyclone separator 3 through the inner extension pipe 5 of the pyrolysis gas to remove a small amount of coke particles contained in the pyrolysis gas.
  • the gas phase separated by the cyclone separator 3 enters the fractionation section 2 for fractionation through the rising pipe 4, and a small amount of coke particles at the bottom of the cyclone separator 3 is discharged through the coke particle discharge pipe 12 and the external coke particle discharge line 14.
  • the cracked gas at the outlet of the liquid furnace contains a lot of heavy components and coke particles. After flashing, a large amount of heavy components and coke particles remain at the bottom of the flash section 1, and are sent to the downstream process through the fuel oil extraction pipeline 11.
  • the cracked gas at the outlet of the gas furnace contains less heavy components and coke particles, and is roughly divided by the cyclone separator 3 to remove most of the coke particles, and directly enters the fractionation section 2 without flashing.
  • the cracked gas at the exit of the liquid furnace after flash evaporation and the cracked gas at the exit of the gas furnace separated by cyclone enter the fractionation section the content of heavy components and coke particles is less, and the heavy components and coke particles in the quenching oil are significantly reduced, and the quenching oil system does not need to be equipped with a pump
  • the pre-filter and the hydrocyclone are separated in two stages. Only the first-stage filter is installed before or after the pump to meet the separation requirements. The equipment investment and occupation are significantly reduced, and the filter operation cycle is increased, which reduces the inspection time. Repair fees.
  • the self-aggregation tendency of the quenching oil is reduced, the temperature is increased, the heat extraction of the quenching oil section of the fractionation tower is increased, and the medium-pressure steam consumption of the device is reduced.
  • Table 1 Listed in Table 1 is the comparison of the temperature, composition and viscosity of the quenching oil at the bottom of the fractionation section or the fractionation tower using the fractionation tower used in Example 1 and the prior art using the fractionation tower under the same cracking raw material conditions. It can be seen that the quench oil at the bottom of the fractionation section of the fractionation tower of the present invention has a higher temperature, a lighter composition, and a significantly lower viscosity, and has relatively excellent performance for stable operation of the fractionation tower and energy saving.
  • the coke cleaning device adopts the coke cleaning tank 17 .
  • the coke cleaning device adopts a coke cleaning tank 18 with built-in several cyclone separators, and several cyclone separators are arranged in an equilateral triangle in the coke cleaning tank.
  • the fractionating tower of the invention has a compact structure, and combines viscosity reduction and fractionation into one; the content of heavy components and coke particles in the quenching oil is reduced, the filter configuration is simple, the equipment investment is low, and the occupation area is reduced; the viscosity of the quenching oil is reduced, which is conducive to improving the Quench oil temperature and improve heat utilization are of great significance for long-term stable operation of ethylene plants and energy saving and consumption reduction.

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

Abstract

本发明涉及一种分馏塔及其用途。该分馏塔包括壳体和设置在壳体内的隔板，所述隔板将壳体内部分隔为下部A段(闪蒸段)和上部B段(分馏段)。本发明的分馏塔结构紧凑，液体炉和气体炉裂解气分开进料，采用闪蒸方法减粘，降低设备投资和占地，改善热量利用，对乙烯装置长周期稳定运行和节能降耗有重要意义。

Description

分馏塔 技术领域
本发明涉及乙烯生产领域，更具体地涉及分馏塔，及其在蒸汽裂解乙烯装置中的用途。
背景技术
传统乙烯装置中液体原料裂解气通过废锅回收热量，经急冷器喷淋急冷油冷却后，与经废锅回收热量的气体原料裂解气混合，进入汽油分馏塔下部急冷油段。其中，通过废锅回收热量的气体原料裂解气(气相，温度200℃左右)焦粒和重组分较少，而液体原料裂解气通过废锅回收热量，经急冷器喷淋急冷油冷却后为两相，温度400℃左右，焦粒和重组分含量大，两股物流物性差别大，混合处理不经济，人为增大了分离负荷。
传统乙烯装置汽油分馏塔急冷油段设置人字挡板或角钢脱除裂解气中的焦粒，急冷油从汽油分馏塔急冷油段底部采出，携带有大量重组分和焦粒。为了脱除急冷油中的焦粒，须在急冷油循环泵前设置泵前过滤器，急冷油循环泵后设置旋液分离器和静置器，设备投资高，且设备数量多，增加了占地面积。
另外，为分离急冷油中的重组分，降低急冷油粘度，提高急冷油温度，传统乙烯装置需要单独设置减粘塔。采用高温气体原料裂解气(温度450-505℃)和高压蒸汽作为汽提介质，将一部分急冷油引入减粘塔进行汽提，重组分从减粘塔塔釜采出，所需中间馏分返回汽油分馏塔。减粘塔的操作温度，设计值通常为250-280℃左右，高温气体原料裂解气热量转移到只有180-200℃的急冷油中，热量利用不够经济。且实际操作中，由于重组分在高温下极易堵塞减粘塔塔釜，减粘塔操作温度要远低于设计值，减粘效果差，为防止急冷油自聚，急冷油的操作温度被迫降低，汽油分馏塔塔釜取热减少，热量上移，塔顶温度升高，容易引起下游急冷水塔内急冷水乳化，影响乙烯装置的稳定运行。由于急冷油作为热源被用来发生稀释蒸汽，急冷油温度下降，发生稀释蒸汽量减少，需要多消耗中压蒸汽发生稀释蒸汽，导致乙烯装置能耗升高。
因此，如何更好地回收裂解气热量，并且实现焦粒脱除和急冷油减粘，仍然是目前亟待解决的技术问题。
发明概述
为解决现有技术中设备投资高、占地面积大、装置运行不稳定、能耗高等问题，本发明提供了一种新型的乙烯装置汽油分馏塔。该汽油分馏塔能够实现更好的焦粒脱除和急冷油减粘，有利于乙烯装置长周期稳定运行和节能降耗。
为了实现上述目的，本发明的第一方面提供了一种分馏塔，所述分馏塔包括壳体和设置在壳体内的隔板，所述隔板将壳体内部分隔为下部A段和上部B段；所述下部A段侧壁至少设置有两个开口，分别与气体管线和混相管线连通；所述下部A段底部与燃料油抽出管线连通；所述上部B段底部设置急冷油抽出口，所述急冷油抽出口与急冷油抽出管线连通；所述隔板上设置有若干开口，分别连接若干升气管，使下部A段和上部B段连通。
本发明的第二方面提供了分馏塔在蒸汽裂解乙烯装置中的用途。
本发明的分馏塔能够实现更好的焦粒脱除和急冷油减粘，有利于乙烯装置长周期稳定运行和节能降耗。特别地，在蒸汽裂解乙烯装置中，该分馏塔具有以下优点：
1)将传统乙烯装置的急冷油段抬高，允许气体原料裂解气管线仍与液体原料裂解气管线保持相同且较低的高度，且避免了气体原料裂解气管线上翻导致的管道下袋，减少长期操作管线中的焦粒积累。
2)气体原料裂解气与液体原料裂解气分开进料，避免焦粒和重组分返混，降低分离负荷，同时又避免气体原料裂解气管线和液体原料裂解气管线两条管线占用空间过大的弊端。
3)塔结构紧凑，将传统乙烯装置的减粘塔与汽油分馏塔合为一体，采用液体原料裂解气经急冷器喷淋急冷油后直接闪蒸的方法减粘。高温气体原料裂解气的高品位热源能够用于发生蒸汽，降低装置能耗。
4)进入分馏区气体重组分和焦粒较少，急冷油中焦粒含量大幅减少，组分变轻，可以简化急冷油过滤器配置，降低投资，减少占地；急冷油粘度降低，有利于提高急冷油温度，改善热量利用，对乙烯装置长周期稳定运行和节能降耗有重要意义。
本发明的其他特征和优点将在随后具体实施方式部分予以详细说明。
附图说明
图1为本发明的分馏塔的第一实施方案的结构示意图。
图2为图1中A-A面的剖视图。
图3为本发明的分馏塔的第二实施方案的结构示意图。
图4为图3中A-A面的剖视图。
图5为本发明的分馏塔的第三实施方案的结构示意图。
图6为图5中A-A面的剖视图。
附图标记说明：
1             闪蒸段
2             分馏段
3             旋风分离器
4             上升管
5             裂解气内伸管
6             气体管线
7             混相管线
8             急冷油抽出口
9             升气管
10            集液包
11            燃料油抽出管线
12            焦粒排放管
13            急冷油抽出管线
14            外部焦粒排放管线
15、16        破涡器
17            清焦罐
18            内置旋风分离器的清焦罐
具体实施方式
下面将更详细地描述本发明的优选实施方式。虽然以下描述了本发明的优选实施方式，然而应该理解，可以以各种形式实现本发明而不应被这里阐述的实施方式所限制。
本发明的分馏塔包括壳体和设置在壳体内的隔板，隔板将壳体内部分隔为下部A段1和上部B段2，下部A段1内设置有清焦设施；下部A段1侧壁至少设置有两个 开口，分别与气体管线6和混相管线7连通；下部A段1底部设置集液包10，集液包10底部与燃料油抽出管线11连通；上部B段2底部设置急冷油抽出口8，急冷油抽出口8与急冷油抽出管线13连通；隔板上设置有若干开口，分别连接若干升气管9，使下部A段1和上部B段2连通；清焦设施通过裂解气内伸管5与气体管线6连通；清焦设施顶部设有上升管4，上升管4向上插入上部B段2；清焦设施底部设有焦粒排放管12，焦粒排放管12向下伸出至塔底，与外部焦粒排放管线14连通。
清焦设施可以为清焦罐、单个旋风分离器和多个旋风分离器的组合中的至少一种。当采用多个旋风分离器的组合时，可将该组合设置于清焦罐内。
裂解气内伸管5可以与清焦设施切线连接。
上部B段2可以设置有内件，内件优选为塔板、填料或其组合；上部B段2可以分为2-4个小段，优选由下至上依次为急冷油段、盘油段和精馏段。
升气管9可以设置在上部B段2内，其出口端的高度可以达到急冷油高液位以上；上升管4在上部B段2可以达到急冷油高液位以上。
上部B段2底部结构可以为封头或集液槽。
上部B段2底部和集液包10底部可以分别设置破涡器15，16。
与气体管线6连通的下部A段1侧壁开口可以不高于与混相管线7连通的下部A段1侧壁开口。
本发明的分馏塔优选地用于既有液体原料又有气体原料的蒸汽裂解乙烯装置，其中气体管线6为输送气体原料裂解气的管线，混相管线7为输送液体原料裂解气和急冷油的管线。
液体原料可以选自碳五及以上轻烃、石脑油、柴油和加氢尾油中的一种或多种；气体原料可以选自乙烷、丙烷、丁烷、炼厂干气和LPG中的一种或多种。
实施例
以下结合附图及实施例，进一步说明本发明。应当理解的是，此处所描述的具体实施方式仅用于说明和解释本发明，并不用于限制本发明。
实施例1
如图1所示，实施例1所采用的分馏塔包括壳体和设置在壳体内的隔板，隔板将壳体内部分隔为下部的闪蒸段1(即下部A段)和上部的分馏段2(即上部B段)， 闪蒸段1内设置有旋风分离器3。闪蒸段1侧壁的两个开口分别与气体管线6和混相管线7连通(与气体管线6连通的闪蒸段1侧壁开口低于与混相管线7连通的闪蒸段1侧壁开口)。闪蒸段1底部设置集液包10，集液包10底部设置第二破涡器16，集液包10底部开口与燃料油抽出管线11连通。旋风分离器3通过裂解气内伸管5与气体管线6连通，旋风分离器3顶部上升管4插入分馏段2，直至急冷油高液位以上，旋风分离器3底部焦粒排放管12向下延伸直至塔底部封头，与外部焦粒排放管线14连通。隔板上设置有若干开口，分别连接若干升气管9，若干升气管9设置在分馏段2内，其出口端的高度达到急冷油高液位以上，分馏段2底部采用封头型式，设置急冷油抽出口8与急冷油抽出管线13连通，最底部设置第一破涡器15。
其中，闪蒸段1不设置分馏内件，分馏段2从下向上设置为急冷油段、盘油段和精馏段，设置塔板内件。
如图2所示，气体管线6与混相管线7呈90°分布，裂解气内伸管5外端与气体管线6连通，内端与旋风分离器3切线连接，分馏段2底部设置5个升气管9与旋风分离器3顶部的上升管4共同形成呈60°间隔分布的6个开口。
分馏塔塔内径13000mm，气体管线6直径为2000mm，混相管线7直径为2600mm，集液包10内径为1200mm，上升管4直径为2000mm，升气管9直径为2500mm，急冷油抽出口直径为1400mm，旋风分离器3直径为4500mm，焦粒排放管12直径为100mm。
在工作过程中，通过废锅回收热量，经急冷器喷淋急冷油冷却后的液体原料裂解气，温度约250-280℃，经混相管线7进入分馏塔闪蒸段1，经闪蒸段1气液分离，所得气相通过分馏段2底部升气管9进入分馏段2，所得焦粒和液相重组分在闪蒸段1底部积累，通过集液包10底部燃料油抽出管线11排出；经废锅回收热量的气体炉出口裂解气，约200℃左右，经气体管线6进入分馏塔闪蒸段1，经裂解气内伸管5进入旋风分离器3，脱除裂解气中含有的少量焦粒/焦粉，旋风分离器3分离后的气相经上升管4进入分馏段2分馏，旋风分离器3底部的少量焦粒通过焦粒排放管12和外部焦粒排放管线14排出。
液体炉出口裂解气含重组分和焦粒较多，经闪蒸，大量重组分和焦粒留在闪蒸段1底部，经燃料油抽出管线11送至下游流程。气体炉出口裂解气含重组分和焦粒较少，经旋风分离器3粗分，脱除大部分焦粒，不经过闪蒸直接进入分馏段2。闪蒸后的液体炉出口裂解气和经旋风分离的气体炉出口裂解气进入分馏段，重组分和焦粒含量较 少，急冷油中重组分和焦粒明显减少，急冷油系统不需要设置泵前过滤器和旋液分离器两级分离，只在泵前或泵后设置一级过滤器即可满足分离要求，设备投资和占地明显降低，且过滤器操作周期有所增长，减少了检维修费用。急冷油自聚倾向降低，温度提高，分馏塔急冷油段取热量上升，减少装置中压蒸汽消耗。
表1中列出的是在相同裂解原料条件下，实施例1采用的分馏塔与现有技术采用分馏塔，分馏段或分馏塔底部急冷油温度、组成和粘度的对比情况。可以看出，本发明的分馏塔分馏段底部急冷油温度较高，组成较轻，粘度明显较小，对于分馏塔稳定操作和节约能耗有较为优异的性能。
表1
项目 实施例1 现有技术
分馏塔釜温(℃) 195.3 195.0
急冷油粘度/(CP) 0.676 7.061
超高压蒸汽量/(t/hr) 537.2 515.0
单位乙烯能耗/(kg标油/t乙烯) 506 520.0
每年操作费用/(万元/万吨乙烯) 基准-27.4 基准
实施例2
如图3、图4所示，采用的分馏塔同实施例1，区别在于：
清焦器采用清焦罐17。
实施例3
如图5、图6所示，采用的分馏塔同实施例1，区别在于：
清焦器采用内置若干旋风分离器的清焦罐18，若干旋风分离器在清焦罐内呈等边三角形排列。
本发明的分馏塔结构紧凑，将减粘与分馏合并为一体；急冷油中重组分和焦粒含量减少，过滤器配置简单，设备投资较低，占地减少；急冷油粘度降低，有利于提高急冷油温度，改善热量利用，对乙烯装置长周期稳定运行和节能降耗具有重要意义。

Claims (13)

  1. 一种分馏塔，其特征在于，所述分馏塔包括壳体和设置在壳体内的隔板，所述隔板将壳体内部分隔为下部A段(1)和上部B段(2)；
    所述下部A段(1)侧壁至少设置有两个开口，分别与气体管线(6)和混相管线(7)连通；所述下部A段(1)底部与燃料油抽出管线(11)连通；
    所述上部B段(2)底部设置急冷油抽出口(8)，所述急冷油抽出口(8)与急冷油抽出管线(13)连通；
    所述隔板上设置有若干开口，分别连接若干升气管(9)，使下部A段(1)和上部B段(2)连通。
  2. 根据权利要求1所述的分馏塔，其中
    所述气体管线(6)为输送气体原料裂解气的管线，所述混相管线(7)为输送液体原料裂解气和急冷油的管线。
  3. 根据权利要求1或2所述的分馏塔，其中
    所述下部A段(1)内设置有清焦设施，所述清焦设施通过裂解气内伸管(5)与所述气体管线(6)连通；所述清焦设施顶部设有上升管(4)，所述上升管(4)向上插入所述上部B段(2)；所述清焦设施底部设有焦粒排放管(12)，所述焦粒排放管(12)向下伸出至塔底，与外部焦粒排放管线(14)连通。
  4. 根据权利要求3所述的分馏塔，其中
    所述清焦设施为清焦罐、单个旋风分离器和多个旋风分离器的组合中的至少一种。
  5. 根据权利要求1或2所述的分馏塔，其中
    所述下部A段(1)底部通过集液包(10)与燃料油抽出管线(11)连通。
  6. 根据权利要求3所述的分馏塔，其中
    所述裂解气内伸管(5)与所述清焦设施切线连接。
  7. 根据权利要求1或2所述的分馏塔，其中
    所述上部B段(2)设置有内件，所述内件优选为塔板、填料或其组合；
    所述上部B段(2)分为2-4个小段，优选由下至上依次为急冷油段、盘油段和精馏段。
  8. 根据权利要求1或2所述的分馏塔，其中
    所述升气管(9)设置在上部B段(2)内，其出口端的高度达到急冷油高液位以上；
    所述上升管(4)在所述上部B段(2)达到急冷油高液位以上。
  9. 根据权利要求1或2所述的分馏塔，其中
    所述上部B段(2)底部结构为封头或集液槽。
  10. 根据权利要求5所述的分馏塔，其中
    所述上部B段(2)底部和所述集液包(10)底部分别设置破涡器(15，16)。
  11. 根据权利要求1或2所述的分馏塔，其中
    与所述气体管线(6)连通的下部A段(1)侧壁开口不高于与混相管线(7)连通的下部A段(1)侧壁开口。
  12. 权利要求1-11中任一项所述的分馏塔在蒸汽裂解乙烯装置中的用途，优选地用于既有液体原料又有气体原料的蒸汽裂解乙烯装置。
  13. 根据权利要求12所述的用途，其中
    所述液体原料选自碳五及以上轻烃、石脑油、柴油和加氢尾油中的一种或多种；
    所述气体原料选自乙烷、丙烷、丁烷、炼厂干气和LPG中的一种或多种。
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