WO2016192306A1 - 一种多重优化的高压分离器及其设计方法和用途 - Google Patents

一种多重优化的高压分离器及其设计方法和用途 Download PDF

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WO2016192306A1
WO2016192306A1 PCT/CN2015/094181 CN2015094181W WO2016192306A1 WO 2016192306 A1 WO2016192306 A1 WO 2016192306A1 CN 2015094181 W CN2015094181 W CN 2015094181W WO 2016192306 A1 WO2016192306 A1 WO 2016192306A1
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pressure separator
cylinder
high pressure
oil
coal
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PCT/CN2015/094181
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English (en)
French (fr)
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李苏安
邓清宇
王坤朋
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北京中科诚毅科技发展有限公司
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Publication of WO2016192306A1 publication Critical patent/WO2016192306A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/02—Foam dispersion or prevention
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/02—Settling tanks with single outlets for the separated liquid
    • 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
    • C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
    • C10G31/06—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by heating, cooling, or pressure treatment

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  • the invention relates to a multi-optimized high-pressure separator, a design method thereof and a use thereof, and belongs to the fields of petrochemical industry and coal chemical industry.
  • the material from the outlet of the slurry bed reactor enters the separator, where the light and heavy components are separated, the light components enter the separator of lower temperature, the heavy components enter the separator of lower pressure, and continue to separate until light
  • the circulating hydrogen and oil and gas in the component are separated, and the solid phase, oil and water in the heavy component are separated. Therefore, the separator, especially the high pressure separator, becomes one of the core devices of the foregoing several processes, and its stability relationship Operational stability to a circulating hydrogen system, a fractionation system, a light hydrocarbon recovery unit, an exhaust gas treatment unit, and a wastewater treatment unit.
  • the common separators in refineries or coal chemical plants generally process gas-liquid two-phase media. Because the purpose is nothing more than gas-liquid separation, the structure is relatively simple. Because of the common feature of heavy oil hydrogenation, direct coal liquefaction and oil-coal mixing reactors, high temperature and high pressure, the reactor outlet material composition is complex and contains many solids, in addition to considering the separation system composed of multiple sets of separators.
  • the separator is specially designed, especially for high pressure separators. When the operating temperature of the high-pressure separator is high, coking phenomenon is likely to occur, resulting in blockage of equipment and even explosion accidents.
  • the operating medium of the separator of hydrogen, oil coal mixing and oil-coal mixing process is a gas-liquid-solid three-phase medium, which requires special structural design.
  • the high pressure separator is both a gas-liquid separation device for the reaction product and a pressure control point for the reaction system. The pressure inside the separator is very large. If the liquid level is not well controlled, the liquid level is too high, which will cause serious liquid phase and solid phase in the gas phase, which will cause the cold exchange equipment to be clogged, the liquid level is too low, and the high pressure system will easily break into the low pressure system. The explosion accident has increased the difficulty of operating the high pressure separator.
  • the present invention provides a multi-optimized high-pressure separator capable of separating light and heavy components of gas-liquid two-phase or gas-liquid-solid three-phase; thereby minimizing the possibility of coking, It can clean the coke in time to avoid blockage; the position of the feed port, the structure of the heavy component outlet and the liquid level design make the feed and discharge more smooth and the equipment It is more convenient and the equipment is more stable.
  • a multi-optimized high-pressure separator characterized in that the high-pressure separator has an aspect ratio of 2.5 to 5.5:1, the feed port is located on the side of the cylinder, and above the liquid level, the liquid level is 10% of the length of the tangent of the cylinder ⁇ 50%, the center line of the feed inlet to the middle line of the cylinder is 15%-40% of the length of the tangential line of the cylinder; the heavy component discharge port is located directly below the cylinder of the high pressure separator, and the light component discharge port is arranged in the cylinder Above; the portion from the lower end of the cylinder to the discharge port of the heavy component adopts a cone structure with a taper angle of 40-120°.
  • the operating temperature is preferably from 30 to 470 ° C, and the operating pressure is preferably from 17 to 22 MPa.
  • the high pressure separator operating medium may be a gas liquid solid three phase mixture.
  • a supplemental hydrogen inlet may also be included, the supplemental hydrogen inlet being located on the side of the cone, and the partial pressure of hydrogen in the high pressure separator being 8-14 MPa.
  • the residence time achievable by the high pressure separator is: 0.5-90 minutes.
  • Each of the outlets of the high pressure separator may preferably be provided with a backwash port.
  • the use of the above multiple optimized high pressure separator is characterized by being used for heavy oil hydrogenation process, coal direct liquefaction process and oil coal mixing process;
  • the heavy oil is heavy crude oil, residual oil, catalytic oil slurry, deoiled asphalt,
  • One or more combinations of coal tar the coal is one or a combination of lignite, bituminous coal, non-sticky coal, and the ratio of oil to coal in the oil-coal mixing process ranges from 97:3-40: 60.
  • the multi-optimized high-pressure separator of the invention is suitable for heavy oil hydrogenation process, coal direct liquefaction process and oil-coal mixing process with high solid content in a high operating pressure environment, and the applicable operating temperature range is large, and It can achieve good separation effect; the measures of supplementing hydrogen can realize that the hydrocarbon molecules do not shrink and coke at higher temperature; the inlet is disposed on the side of the cylinder above the liquid surface instead of the upper end, which can make the liquid phase coke.
  • the plugging of the feed port the separation does not cause the reflux to hinder the feed, and the range of the aspect ratio is moderate, so that the inlet port arrangement is more convenient, and the interface between the gas-liquid separation and the floor space is well balanced.
  • the cost is controllable; the liquid level is set in the range of 15-50%, which makes the operation more stable, avoiding the liquid level being too high, the light component is entrained with too much heavy component or the liquid surface is too low, and the light component is discharged from the lower end;
  • the taper is set near the mouth and the outlet is placed at the bottom of the cone, so that heavy components such as liquid solids can be more easily guided and separated by sliding, even if it is occasionally coked, the coke We will leave the separator without clogging the discharge port along with the heavies.
  • hydrogen is added to the high-pressure separator.
  • the hydrogen partial pressure is positively correlated with the operating pressure and operating temperature of the high-pressure separator, and the partial pressure of hydrogen is 8-14 MPa.
  • Figure 1 is a schematic view of a reactor according to an embodiment of the present invention, and the numbers in the figures are listed as follows:
  • 1-Separator body 2-feed line, 3-liquid surface, 4-light component discharge port, 5-heavy component discharge port, 6-light component outlet backwash port, 7-light component outlet Backwash port, 8-heavy component outlet backwash port, 9-heavy component outlet backwash port, 10-hydrogen inlet, 11-hydrogen inlet, 12-heavy component outlet backwash port, 13-heavy component outlet backflush port.
  • the separator is a high temperature and high pressure separator in a coal-oil mixing process.
  • the heavy component discharge port 5 is located directly below the cylinder of the high pressure separator, and the light component discharge port 4 is disposed above the cylinder; the lower end of the cylinder to the portion of the heavy component discharge port 5 With a cone structure, the cone angle is 90°.
  • the hydrogen inlet 11 is located at the side of the cone, and the hydrogen partial pressure is controlled between 11-13 MPa.
  • Light component outlet backwash ports 6, 7 and heavy component outlet backflush ports 8, 9, 12, 13 are provided adjacent the light component discharge port 4 and the heavy component discharge port 5, respectively.
  • the embodiment proves that it is suitable for use in a high operating pressure environment, and can achieve a good separation effect; the measures for supplementing hydrogen can realize that the hydrocarbon molecules do not shrink and coke at a higher temperature;
  • the inlet of the material pipe 2 is disposed on the side of the cylinder above the liquid level instead of the upper end, so that once the liquid phase is coked, the inlet is not blocked, and the separated return does not cause the feed to be hindered, and the aspect ratio is
  • the moderate range makes the inlet more convenient and takes into account the separation effect and the volume of the equipment, thus optimizing the equipment cost; the height of the liquid level 3 makes the operation more stable, so that the light components are entrained with too much heavy components or light components from The lower end is discharged; the heavy component discharge port 5 is arranged in a tapered shape and the outlet is arranged on the bottom of the cone, so that heavy components such as liquid solids are more easily guided and separated by high efficiency, even if occasionally coking, the coke will be accompanied by heavy components
  • each outlet is provided with a backwashing point to enable the coke material to be cleaned in a timely and powerful manner, which improves the operation of the device. Stability and operational cycle, the overall operation is very smooth, there is no residue of coke; the use of heavy diesel oil or wax flushing coke, since the backwashing substance is a product, it will not introduce impurities and increase costs.

Abstract

一种多重优化的高压分离器及其设计方法和用途，分离器的长径比为2.5～5.5：1，进料口位于筒体侧面，且在液面以上，液面高度为筒体切线长度的10％～50％，进料口中心线至筒体中间线为筒体切线长度的15％-40％；重组分出料口（5）位于高压分离器筒体正下方，轻组分出料口（4）设置在筒体上方；筒体下端至重组分出料口（5）的部分采用锥形体结构，锥角为40-120°。

Description

一种多重优化的高压分离器及其设计方法和用途 技术领域
本发明涉及一种多重优化的高压分离器及其设计方法和用途，属于石油化工和煤化工领域。
背景技术
近年来，随着全球原油开采量的不断增加和常规原油储量的不断减少，原油劣质化趋势越来越严重，与此同时，市场对轻质油的需求不断增加。于是，重油浆态床加氢工艺、煤直接液化工艺和煤混炼工艺越来越受到重视，这几种技术都需要采用一种高效地高压分离器，本设备安装在浆态床反应器下游，来自浆态床反应器出口的物料进入分离器，轻重组分在此得以分离，轻组分进入温度低一级的分离器，重组分进入压力低一级的分离器，继续分离，直至轻组分中的循环氢和油气实现分离，重组分中的固相、油和水实现分离，所以，分离器，尤其是高压分离器成为前述几种工艺的核心设备之一，它的稳定性关系到循环氢系统、分馏系统、轻烃回收装置、尾气处理装置、废水处理装置等的操作稳定性。
目前炼油厂或煤化工厂常见的分离器一般是处理气液两相介质的，由于目的无外乎实现气液分离，所以结构相对简单。由于重油加氢、煤直接液化和油煤混炼反应器的共同特点是高温高压，反应器出口物料组份复杂，还包含许多固体，除了考虑使用多组分离器组成的分离系统外，还要对分离器进行特殊设计，尤其是高压分离器。在高压分离器的操作温度较高时，还容易发生结焦现象，造成设备堵塞，甚至发生爆炸事故，所以需要做到尽量避免结焦，同时还要具备及时处理结焦物的功能，重油浆态床加氢、油煤混炼和油煤混炼工艺的分离器的操作介质是气液固三相介质，需要特殊的结构设计。另外，高压分离器既是反应产物的气液分离设备，又是反应系统的压力控制点。分离器内压力非常大，如液面控制不好，液面过高，会造成气相夹带液相和固相严重，而造成冷换设备堵塞，液面过低，容易发生高压系统窜入低压系统而发生爆炸事故，增加了高压分离器的操作难度。
发明内容
为了解决现有技术的问题，本发明提供一种多重优化的高压分离器，能够实现气液两相或气液固三相的轻重组分分离；既最大程度地降低了结焦的可能性性，又能够及时地清理结焦物避免发生堵塞；进料口位置、重组分出口结构和液位设计使得进出料更加通畅、设备操 作更加方便、设备运行更加稳定。
本发明的技术方案：
一种多重优化的高压分离器，其特征在于高压分离器长径比为2.5～5.5：1，进料口位于筒体侧面，且在液面以上，液面高度为筒体切线长度的10％～50％，进料口中心线至筒体中间线为筒体切线长度的15％-40％；重组分出料口位于高压分离器筒体正下方，轻组分出料口设置在筒体上方；筒体下端至重组分出料口的部分采用锥形体结构，锥角为40-120°。
操作温度优选是30-470℃，操作压力优选是17-22MPa。
所述高压分离器操作介质可以为气液固三相混合物。
还可以包括补充氢气入口，所述补充氢气入口位于锥形体的侧部，高压分离器内的氢分压为8-14MPa。
高压分离器可实现的停留时间是：0.5-90分钟。
所述高压分离器的各出口可优选的设置反冲洗口。
优选的使用产物中的蜡油或重柴油冲洗。
上述多重优化的高压分离器的用途，其特征在于用于重油加氢工艺、煤直接液化工艺和油煤混炼工艺；所述重油为重质原油、渣油、催化油浆、脱油沥青、煤焦油的一种或者多种组合，所述煤为褐煤、烟煤、不粘煤中的一种或者多种组合，所述油煤混炼工艺中油与煤的比例范围为97:3-40:60。
还包括上述多重优化的高压分离器的设计方法。
技术效果：
本发明的一种多重优化的高压分离器适用于较高操作压力的环境下固体含量较多的重油加氢工艺、煤直接液化工艺和油煤混炼工艺，适用的操作温度范围较大，并且能实现很好的分离效果；设置补充氢气的措施，能够实现在较高温度下，烃分子不缩聚结焦；进口设置在液面上方的筒体侧面而不是上端，能够使得一旦液相发生结焦不至于堵塞进料口，另外不会使得分离出的发生回流而阻碍进料，长径比的范围适中使得进料口布置更加方便，且使得气液分离的界面与占地面积达到良好的平衡，成本可控；液面高度设置在15-50％范围，使得操作更加稳定，避免了液面过高轻组分夹带重组分过多或者液面过低轻组分从下端流出；重组分出料口附近设置为锥形且出口设置于锥底，使得液固等重组分更容易被高效地引导滑落分离出去，即便是偶尔结焦，结焦物也会随重组分一起离开分离器而不会堵塞出料口。
为保证氢分压，在操作温度高于300℃时，要向高压分离器内补充氢气，氢分压与高压分离器操作压力和操作温度正相关，氢分压为8-14MPa。
高压分离器各出口设置反冲洗口，使用蜡油或重柴油冲洗结焦，使得结焦物得到及时的 清理，提高了设备的操作稳定性和运行周期；由于反冲洗物质是产物，因此不会引入杂质和增加成本。
附图说明
图1为本发明实施例的反应器简图，图中各标号列示如下：
1-分离器主体，2-进料管道，3-液面，4-轻组分出料口，5-重组分出料口，6-轻组分出口反冲洗口，7-轻组分出口反冲洗口，8-重组分出口反冲洗口，9-重组分出口反冲洗口，10-氢气进口，11-氢气进口，12-重组分出口反冲洗口，13-重组分出口反冲洗口。
具体实施方式
为进一步阐述本发明的具体特征，将结合图1与具体实施例加以说明。
实施例
如图1所示，本分离器为油煤混炼工艺中的高温高压分离器。
进入分离器主体1的介质为气液固三相混合物；分离器操作温度为455℃，操作压力为18.7MPa左右，分离器设计停留时间为2分钟；分离器筒体切线长度为L＝3m，内径长度为0.25L；进料管道2的进口位于筒体侧面且在液面以上，距离筒体上部为0.25L，液面3高度为0.25-0.4L之间波动(图中状态为3L)，并设置液面控制重组分流出量；重组分出料口5位于高压分离器筒体正下方，轻组分出料口4设置在筒体上方；筒体下端至重组分出料口5的部分采用锥形体结构，锥角为90°。包括补充氢气的进口，氢气进口11位于锥形体的侧部，氢分压控制在11-13MPa间。在轻组分出料口4和重组分出料口5附近分别设置轻组分出口反冲洗口6、7和重组分出口反冲洗口8、9、12、13。
本实施例经过长时间运行，证明其适用于较高操作压力的环境下，并且能实现很好的分离效果；设置补充氢气的措施，能够实现在较高温度下，烃分子不缩聚结焦；进料管道2的进口设置在液面上方的筒体侧面而不是上端，能够使得一旦液相发生结焦不至于堵塞进料口，另外不会使得分离出的发生回流而阻碍进料，长径比的范围适中使得进料口在布置更加方便且兼顾分离的效果和设备的体积，从而优化设备成本；液面3的高度使得操作更加稳定，不至于轻组分夹带重组分过多或者轻组分从下端流出；重组分出料口5附近设置为锥形且出口设置于锥底，使得液固等重组分更容易被高效地引导滑落分离出去，即便是偶尔结焦，结焦物也会随重组分一起滑落离开分离器而不会堵塞出料口；各出口设置反冲洗点使得结焦物得到及时有力的清理，提高了设备的操作稳定性和运行周期，总体的运行十分平稳，没有结焦物的残留；使用蜡油或重柴油冲洗结焦，由于反冲洗物质是产物，因此不会引入杂质和增加成本。
以上所述仅为本发明较佳的具体实施方式，但本发明的保护范围并不局限于此，任何熟 悉本技术领域的技术人员在本发明揭露的技术范围内，可轻易想到的变化或替换，都应涵盖在本发明的保护范围之内。因此，本发明的保护范围应该以权利要求书的保护范围为准。

Claims (9)

  1. 一种多重优化的高压分离器，其特征在于高压分离器长径比为2.5～5.5：1，进料口位于筒体侧面，且在液面以上，液面高度为筒体切线长度的10％～50％，进料口中心线至筒体中间线为筒体切线长度的15％-40％；重组分出料口位于高压分离器筒体正下方，轻组分出料口设置在筒体上方；筒体下端至重组分出料口的部分采用锥形体结构，锥角为40-120°。
  2. 根据权利要求1所述的一种多重优化的高压分离器，其特征在于操作温度是30-470℃，操作压力是17-22MPa。
  3. 根据权利要求1所述的一种多重优化的高压分离器，其特征在于所述高压分离器操作介质为气液固三相混合物。
  4. 根据权利要求1所述的一种多重优化的高压分离器，其特征在于还包括补充氢气入口，所述补充氢气入口位于锥形体的侧部，高压分离器内的氢分压为8-14MPa。
  5. 根据权利要求1所述的一种多重优化的高压分离器，其特征在于高压分离器停留时间是：0.5-90分钟。
  6. 根据权利要求1所述的一种多重优化的高压分离器，其特征在于所述高压分离器的各出口设置反冲洗口。
  7. 根据权利要求6所述的一种多重优化的高压分离器，其特征在于使用产物中的蜡油或重柴油冲洗。
  8. 根据权利要求1-7任一所述的一种多重优化的高压分离器的用途，其特征在于用于重油加氢工艺、煤直接液化工艺和油煤混炼工艺；所述重油为重质原油、渣油、催化油浆、脱油沥青、煤焦油的一种或者多种组合，所述煤为褐煤、烟煤、不粘煤中的一种或者多种组合，所述油煤混炼工艺中油与煤的比例范围为97:3-40:60。
  9. 一种多重优化的高压分离器的设计方法，其特征在于高压分离器长径比为2.5-5.5：1，进料口位于筒体侧面，且在液面以上，液面高度为筒体切线长度的10％～50％，进料口中心线至筒体中间线为筒体切线长度的15％-40％；重组分出料口位于高压分离器筒体正下方，轻组分出料口设置在筒体上方；重组分出料口采用锥形体结构，锥角为40-120°。
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CN104888500B (zh) * 2015-06-03 2017-08-25 北京中科诚毅科技发展有限公司 一种多重优化的高压分离器及其设计方法和用途
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Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB660113A (en) * 1944-02-22 1951-10-31 Directie Staatsmijnen Nl Process and apparatus for separation of gaseous mixtures by fractional condensation under pressure
WO2007096410A2 (de) * 2006-02-23 2007-08-30 Mann+Hummel Gmbh Druckwellenbetriebene abscheidung von flüssig- oder feststoffen aus einem medium und vorrichtungen zur durchführung der abscheidung
CN200987927Y (zh) * 2006-11-17 2007-12-12 上海动力设备有限公司 冲击式分离器
CN101890254A (zh) * 2009-05-22 2010-11-24 新奥科技发展有限公司 用于高温高压复杂流体的分离系统和分离方法
CN102794034A (zh) * 2012-08-27 2012-11-28 神华集团有限责任公司 一种高温高压分离器
CN202724761U (zh) * 2012-08-27 2013-02-13 神华集团有限责任公司 一种带有防沉积结构的高温高压分离器
CN104888500A (zh) * 2015-06-03 2015-09-09 北京中科诚毅科技发展有限公司 一种多重优化的高压分离器

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN204767628U (zh) * 2015-06-03 2015-11-18 北京中科诚毅科技发展有限公司 一种多重优化的高压分离器

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB660113A (en) * 1944-02-22 1951-10-31 Directie Staatsmijnen Nl Process and apparatus for separation of gaseous mixtures by fractional condensation under pressure
WO2007096410A2 (de) * 2006-02-23 2007-08-30 Mann+Hummel Gmbh Druckwellenbetriebene abscheidung von flüssig- oder feststoffen aus einem medium und vorrichtungen zur durchführung der abscheidung
CN200987927Y (zh) * 2006-11-17 2007-12-12 上海动力设备有限公司 冲击式分离器
CN101890254A (zh) * 2009-05-22 2010-11-24 新奥科技发展有限公司 用于高温高压复杂流体的分离系统和分离方法
CN102794034A (zh) * 2012-08-27 2012-11-28 神华集团有限责任公司 一种高温高压分离器
CN202724761U (zh) * 2012-08-27 2013-02-13 神华集团有限责任公司 一种带有防沉积结构的高温高压分离器
CN104888500A (zh) * 2015-06-03 2015-09-09 北京中科诚毅科技发展有限公司 一种多重优化的高压分离器

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