CN1114458C - Crude oil atmospheric vacuum distillation method with deep stripping process - Google Patents
Crude oil atmospheric vacuum distillation method with deep stripping process Download PDFInfo
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Abstract
本发明属于一种干式操作的原油蒸馏分离方法，其特征是减压塔侧并联一洗涤罐，减压蒸馏塔的进料段与汽提段由液封隔离分布器隔开，汽提段的油气通过连通管进入洗涤罐的下部，取自减压塔减三线出料的吸收油经冷却后由洗涤罐上部进入向下喷淋与向上的油气逆向换热和传质，洗涤罐的罐顶油气出料返回减压塔的上部，罐底出料作为洗涤油返回减压塔。增设的洗涤罐使得减压塔汽提段的渣油经历了一个深汽提的过程，一般可使减压渣油的拔出率在原有的基础上提高3%～6%。
The invention belongs to a crude oil distillation and separation method of dry operation, which is characterized in that a washing tank is connected in parallel to the side of the vacuum distillation tower, the feed section and the stripping section of the vacuum distillation tower are separated by a liquid-sealed isolation distributor, and the stripping section The oil and gas enter the lower part of the washing tank through the connecting pipe, and the absorption oil taken from the decompression tower minus the third line is cooled and then enters the downward spraying and upward oil and gas reverse heat exchange and mass transfer from the upper part of the washing tank. The oil and gas output from the top returns to the upper part of the vacuum tower, and the output from the bottom of the tank returns to the vacuum tower as washing oil. The additional washing tank makes the residual oil in the stripping section of the vacuum tower go through a deep stripping process, which can generally increase the extraction rate of the vacuum residual oil by 3% to 6% on the original basis.
Description
本发明属于一种原油的蒸馏分离方法。The invention belongs to a method for distillation and separation of crude oil.
原油的常减压蒸馏过程被称为石油炼制的龙头，其能耗的大小以及分离效率直接影响石油炼制的经济效益，因此常减压蒸馏工艺的研究历来受到石油炼制研究领域的关注。早期的湿式减压蒸馏因能耗过大而逐渐被干式操作所取代，干式操作技术在节能方面效果是显著的，但也存在明显的缺陷。由于采用干式操作的常减压装置中的减压塔不存在提馏段，减压塔的拔出率基本取决于由常压渣油的进料温度以及进料层的真空度决定的一次汽化分离，缺乏提馏段的进一步汽提分离，故干式操作一般拔出率较低。为弥补这一缺陷，现有技术中已有不少改进的方案提出。如CN 96101722.8专利申请提出了一种带提馏段的原油常减压工艺方法，该方法将传统的常压塔由一个提馏塔和一个精馏塔取代，原油经换热后由提馏塔的塔顶进料闪蒸，产生的蒸汽进入原油精馏塔的指定位置。在原油提馏塔内原油不汽化的液相向下流动与塔釜上升的蒸汽进行接触和传质，原油提馏塔塔底油经加热后返回提馏塔。提馏塔的不同位置抽出四股汽相侧线分别进入精馏塔的四个相应位置，而精馏塔的四个不同位置采出四个侧线作为不同轻质油产品，精馏塔的塔底渣油经加热后进入减压塔。该专利申请提出的方法与传统的常减压蒸馏工艺相比，常压蒸馏引入了提馏过程，分离效果明显改善，整个常减压蒸馏过程的热量利用合理，轻质油的收率也有所提高。但问题是该方法是通过引入串联的塔设备来实现减少能耗和提高轻质油收率的，对于新建装置而言，要求有较高的设备投资，对于改造已有常减压装置来说，也因投资高和改动过大等原因而难以适用。The atmospheric and vacuum distillation process of crude oil is known as the leader of petroleum refining. Its energy consumption and separation efficiency directly affect the economic benefits of petroleum refining. Therefore, the research on atmospheric and vacuum distillation process has always been concerned by the field of petroleum refining research. . The early wet vacuum distillation was gradually replaced by dry operation due to excessive energy consumption. The dry operation technology has a remarkable effect on energy saving, but it also has obvious defects. Since there is no stripping section in the vacuum tower in the atmospheric and vacuum unit with dry operation, the extraction rate of the vacuum tower basically depends on the primary pressure determined by the feed temperature of the atmospheric residue and the vacuum degree of the feed layer. Vaporization separation lacks further stripping and separation in the stripping section, so dry operation generally has a low extraction rate. In order to make up for this defect, many improved solutions have been proposed in the prior art. For example, CN 96101722.8 patent application proposes a crude oil atmospheric and vacuum process method with a stripping section, which replaces the traditional atmospheric tower with a stripping tower and a rectifying tower, and the crude oil is passed through the stripping tower after heat exchange. The top feed of the column is flashed, and the generated steam enters the designated position of the crude oil distillation column. In the crude oil stripping tower, the non-vaporized liquid phase of the crude oil flows downward to contact and mass transfer with the steam rising from the bottom of the tower, and the bottom oil of the crude oil stripping tower returns to the stripping tower after being heated. Four vapor phase side streams are drawn from different positions of the stripping tower into four corresponding positions of the rectification tower, and four side streams are extracted from four different positions of the rectification tower as different light oil products, and the bottom residue of the rectification tower is After the oil is heated, it enters the vacuum tower. Compared with the traditional atmospheric and vacuum distillation process, the method proposed in this patent application introduces the stripping process, the separation effect is significantly improved, the heat utilization of the entire atmospheric and vacuum distillation process is reasonable, and the yield of light oil is also improved. improve. But the problem is that this method reduces energy consumption and increases the yield of light oil by introducing series-connected tower equipment. For new equipment, a relatively high investment in equipment is required. For the transformation of existing atmospheric and vacuum equipment , It is also difficult to apply due to reasons such as high investment and excessive changes.
本发明的目的是提供一种新的原油常减压蒸馏分离方法，它是在干式减压操作的基础上对减压塔设备进行并不很大的改动，而且在未明显增加能耗的前提下使得减压塔的拔出率有较为显著的提高。The purpose of this invention is to provide a kind of new crude oil atmospheric and vacuum distillation separation method, it is to carry out not very big change to vacuum tower equipment on the basis of dry depressurization operation, and without significantly increasing energy consumption Under the premise, the pull-out rate of the vacuum tower has been significantly improved.
本发明提供的原油常减压蒸馏分离方法包括原油的常压蒸馏前加热、常压蒸馏、减压蒸馏前加热、减压蒸馏等过程。减压蒸馏为干式操作，常压蒸馏前加热、常压蒸馏、减压蒸馏前加热等过程的设备和工艺与传统的方法并无差异，其改进点在于减压蒸馏减压蒸馏塔侧并联一塔顶设有真空增压器的洗涤罐，减压蒸馏塔的进料段与汽提段由液封隔离分布器隔开，汽提段的油气通过连通管进入洗涤罐的下部，取自减压塔减三线出料的馏分油经冷却后由洗涤罐上部进入向下喷淋与向上的油气逆向换热和传质，洗涤罐的罐顶油气出料经真空增压器返回减压塔的上部，罐底出料作为洗涤油返回减压塔。The crude oil atmospheric and vacuum distillation separation method provided by the present invention includes processes such as heating before atmospheric distillation, atmospheric distillation, heating before vacuum distillation, and vacuum distillation of crude oil. Vacuum distillation is a dry operation. The equipment and process of heating before atmospheric distillation, atmospheric distillation, and heating before vacuum distillation are no different from the traditional method. The improvement is that the vacuum distillation column is connected in parallel A washing tank with a vacuum booster is installed on the top of the tower. The feed section of the vacuum distillation tower is separated from the stripping section by a liquid-sealed isolation distributor. The oil and gas in the stripping section enters the lower part of the washing tank through a connecting pipe and is taken from The distillate oil discharged from the decompression tower minus the third line is cooled and then enters the downward spray from the upper part of the washing tank and reverses heat exchange and mass transfer with the upward oil and gas, and the oil and gas discharge from the tank top of the washing tank returns to the decompression tower through the vacuum booster The upper part of the tank bottom is returned to the vacuum tower as washing oil.
为了分别提高洗涤罐和减压塔汽提段中液滴的蒸发表面，洗涤罐中和减压塔汽提段可设有结构填料或格栅类填料。In order to increase the evaporation surface of the droplets in the washing tank and the stripping section of the vacuum tower respectively, the washing tank and the stripping section of the vacuum tower can be provided with structural packing or grid packing.
减压塔汽提段至洗涤罐下部连通管的管径视洗涤罐的负荷而定，发明人认为连通管中的油气速度控制在0.4～0.6马赫数是合适的，而洗涤罐顶的残压控制在10～30mm Hg较宜。The pipe diameter of the connecting pipe from the stripping section of the vacuum tower to the lower part of the washing tank depends on the load of the washing tank. The inventor believes that it is appropriate to control the oil and gas velocity in the connecting pipe at Mach 0.4-0.6, while the residual pressure on the top of the washing tank It is better to control it at 10-30mm Hg.
不难理解，本发明提供的原油常减压蒸馏方法建议增设的洗涤罐可设计成较小的体积，在一般的常减压装置中可以方便地安置，对原有装置的改动也极为有限，因而非常适合对现有的一般干式操作的常减压装置实施改造。而洗涤罐顶部的真空增压器抽吸的可凝油气可设计为较小的数值，因此蒸汽耗量极低。与现有一般的干式操作原油常减压蒸馏方法相比，本发明的积极效果是显著的，上述在减压塔侧线增设的洗涤罐使得减压塔汽提段的渣油经历了一个深汽提的过程，一般可使减压渣油的拔出率在原有的基础上提高3％～6％。It is not difficult to understand that the crude oil atmospheric and vacuum distillation method provided by the present invention suggests that the additional washing tank can be designed to have a smaller volume, which can be easily installed in a general atmospheric and vacuum device, and the modification of the original device is also extremely limited. Therefore, it is very suitable for retrofitting the existing atmospheric and vacuum devices with general dry operation. The condensable oil and gas sucked by the vacuum booster on the top of the washing tank can be designed to be a small value, so the steam consumption is extremely low. Compared with the existing general dry operation crude oil atmospheric and vacuum distillation method, the positive effect of the present invention is remarkable, and the above-mentioned washing tank added at the side line of the vacuum tower makes the residue oil in the stripping section of the vacuum tower experience a deep process. The stripping process can generally increase the extraction rate of vacuum residue by 3% to 6% on the original basis.
附图1及附图2展示了本发明的两个实施方案。Accompanying drawing 1 and accompanying drawing 2 have shown two embodiments of the present invention.
附图1为实施例1的原油常减压蒸馏流程中减压塔及增设的洗涤罐部分的流程示意图；Accompanying drawing 1 is the schematic flow sheet of vacuum tower and the washing tank part of setting in the crude oil atmospheric and vacuum distillation flow process of embodiment 1;
附图2为实施例2的原油常减压蒸馏流程中减压塔及增设的洗涤罐部分的流程示意图。Accompanying drawing 2 is the schematic flow chart of the vacuum tower and the added washing tank part in the crude oil atmospheric and vacuum distillation flow process of embodiment 2.
由于本发明对于传统的干式操作原油常减压蒸馏流程除减压塔外其他部分不作变动，仅给出减压塔及增设的洗涤罐流程并不影响该技术领域一般技术人员对本发明的理解。Since the present invention does not change other parts of the traditional dry operation crude oil atmospheric and vacuum distillation process except the vacuum tower, only the vacuum tower and the additional washing tank process are given without affecting the understanding of the present invention by those skilled in the art .
在附图1所示的实施例中，洗涤罐2并联于减压塔1，其高度接近于减压塔减三线侧线出料的位置。洗涤罐2的顶部设有真空增压器3，减压塔的进料段与汽提段由液封隔离分布器4隔开，汽提段中的油气通过连通管5由洗涤罐下部的油气进料口2a进入洗涤罐。取自减压塔减三线出料的吸收油经冷却后由洗涤罐上部的洗涤油进口2b进入洗涤罐，上升的油气与向下喷淋的洗涤油逆向换热和传质。洗涤罐底出料口2c的出料利用液位差返回减压塔的过汽化油集油箱，而洗涤罐顶部油气出口2d出料的油气则返回减压塔的减二线出料与减三线回流洗涤油进料之间。In the embodiment shown in accompanying drawing 1, washing tank 2 is connected in parallel with decompression tower 1, and its height is close to the position of decompression tower minus three lines side line discharge. The top of the washing tank 2 is equipped with a vacuum booster 3, and the feed section of the decompression tower is separated from the stripping section by a liquid-sealed isolation distributor 4. The oil and gas in the stripping section pass through the connecting pipe 5 from the oil and gas at the bottom of the washing tank. Feed port 2a enters the washing tank. The absorption oil taken from the decompression tower minus the third line is cooled and then enters the washing tank through the washing oil inlet 2b on the upper part of the washing tank, and the rising oil gas and the washing oil sprayed downward are reversed for heat exchange and mass transfer. The discharge from the discharge port 2c at the bottom of the washing tank is returned to the over-vaporized oil collection tank of the decompression tower using the liquid level difference, while the oil and gas discharged from the oil and gas outlet 2d on the top of the washing tank is returned to the discharge of the second line and the reflux of the third line of the decompression tower Wash between oil feeds.
减压塔汽提段中以及洗涤罐中均设有填料。Packing is provided in the stripping section of the vacuum tower and in the washing tank.
实施例1的优点是洗涤罐过汽化油的出料可利用液位差返回减压塔，而缺点是连通管5有较长的长度，这将造成洗涤罐中的真空度损失。The advantage of embodiment 1 is that the discharge of the overvaporized oil in the washing tank can be returned to the decompression tower by using the liquid level difference, but the disadvantage is that the connecting pipe 5 has a long length, which will cause the loss of vacuum in the washing tank.
在附图2所示的实施例中，洗涤罐2并联于减压塔1的汽提段侧。洗涤罐2的顶部设有真空增压器3。减压塔的进料段与汽提段由液封隔离分布器4隔开，汽提段中的油气通过连通管6由洗涤罐下部的油气进料口2a进入洗涤罐。取自减压塔减三线出料的馏份油由洗涤罐上部的洗涤油进口2b进入洗涤罐，上升的油气与向下喷淋的洗涤油逆向换热和传质。洗涤罐底出口2c的出料通过油泵7作为轻洗涤油打回减压塔，而洗涤罐顶部油气出口2d出料的油气则返回减压塔的减二线出料与减三线回流洗涤油进料之间。减压塔汽提段中以及洗涤罐中均设有填料。In the embodiment shown in accompanying drawing 2, washing tank 2 is connected in parallel on the stripping section side of decompression tower 1. The top of the washing tank 2 is provided with a vacuum booster 3 . The feed section and the stripping section of the vacuum tower are separated by a liquid-sealed isolation distributor 4, and the oil and gas in the stripping section enter the washing tank from the oil and gas feeding port 2a at the lower part of the washing tank through the connecting pipe 6. The distillate oil taken from the decompression tower minus the third line discharges into the washing tank through the washing oil inlet 2b on the upper part of the washing tank, and the rising oil gas and the washing oil sprayed downward exchange heat and mass transfer in reverse. The discharge from the outlet 2c at the bottom of the washing tank is sent back to the vacuum tower through the oil pump 7 as light washing oil, while the oil and gas discharged from the oil and gas outlet 2d at the top of the washing tank is returned to the discharge of the second line of the vacuum tower and the feed of the backflow washing oil of the third line between. Packing is provided in the stripping section of the vacuum tower and in the washing tank.
实施例2的优点是连通管6较短，避免了洗涤罐中的真空度损失，但须增设一油泵。The advantage of embodiment 2 is that the connecting pipe 6 is relatively short, which avoids the vacuum loss in the washing tank, but an oil pump must be added.
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| CN99116877A CN1114458C (en) | 1999-09-15 | 1999-09-15 | Crude oil atmospheric vacuum distillation method with deep stripping process |
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| CN99116877A CN1114458C (en) | 1999-09-15 | 1999-09-15 | Crude oil atmospheric vacuum distillation method with deep stripping process |
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| CN1114458C true CN1114458C (en) | 2003-07-16 |
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| CN101987049B (en) | 2009-07-30 | 2014-10-01 | 上海微创医疗器械（集团）有限公司 | Method and device for loading medicine and/or polymers on medical appliance |
| CN102125474B (en) | 2010-01-19 | 2012-10-31 | 微创医疗器械(上海)有限公司 | Method and device for loading medicines and/or polymers on medical equipment |
| CN101810936B (en) * | 2010-04-20 | 2011-08-10 | 上海通凌新能源科技发展有限公司 | Safe coupling equipment of atmospheric distillation system and reduced pressure distillation system and using method thereof |
| CN102443407B (en) * | 2010-10-13 | 2014-04-16 | 中国石油化工股份有限公司 | Crude oil deep drawing process method |
| CN102676204A (en) * | 2012-05-16 | 2012-09-19 | 海工英派尔工程有限公司 | Flash distillation washing method for atmospheric and vacuum distillation of crude oil |
| CN102964228B (en) * | 2012-12-06 | 2014-12-24 | 广西京桂香料有限公司 | Natural cinnamaldehyde extraction process |
| CN102964229B (en) * | 2012-12-06 | 2015-04-29 | 广西京桂香料有限公司 | Natural cinnamaldehyde extraction device |
| CN107653005B (en) * | 2016-07-25 | 2019-08-20 | 郑莹 | Decompression distillation system and vacuum distillation deep drawing technique |
| CN112708443B (en) * | 2019-10-24 | 2022-11-15 | 中国石化工程建设有限公司 | Catalytic slurry oil distillation tower and method for intensively washing catalytic slurry oil |
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| EP0502404A1 (en) * | 1991-03-04 | 1992-09-09 | Federico Esteban Dr. Lantos | Method for decreasing the level of contamination of fuels |
| CN1072200A (en) * | 1991-11-03 | 1993-05-19 | 史万年 | A kind of process flow for petroleum distillation |
| CN1156751A (en) * | 1996-02-09 | 1997-08-13 | 清华大学 | Composite Process of Atmospheric and Vacuum Distillation of Crude Oil with Stripping Section |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0502404A1 (en) * | 1991-03-04 | 1992-09-09 | Federico Esteban Dr. Lantos | Method for decreasing the level of contamination of fuels |
| CN1072200A (en) * | 1991-11-03 | 1993-05-19 | 史万年 | A kind of process flow for petroleum distillation |
| CN1156751A (en) * | 1996-02-09 | 1997-08-13 | 清华大学 | Composite Process of Atmospheric and Vacuum Distillation of Crude Oil with Stripping Section |
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