技术领域technical field
本发明涉及石油化工领域，具体地，涉及一种处理重质油的方法。The invention relates to the field of petrochemical industry, in particular to a method for processing heavy oil.
背景技术Background technique
萃取塔是溶剂萃取工艺的关键设备，它的通量和效率的高低决定了整个工艺设备的规模和大小。溶剂萃取的萃取塔分成几个区域，每个区域有其特定的作用，最下部一般作为重组分的沉降区；溶剂入口附近是沥青凝聚和洗涤区，在那里有新鲜溶剂注入以洗涤凝聚的重组分，使吸附在重组分上的油分进一步分离出来；在溶剂与原料渣油入口这一区间将需要的油分溶解出来，而富含沥青质或胶质的重组分被析出；原料油入口以上的部分是脱沥青油的提纯区，它显示类似选择性溶剂的作用，把已经溶解在脱沥青溶液中的非理想组分进一步除去，以保证脱沥青油质量。现有的溶剂萃取工艺中对原料油进萃取塔的方式一般是由塔的中上部固定位置进入，依靠采用一段或者两段的工艺调节脱沥青油的质量。但是，采用这种方式并没有依据加工的原料的特性。The extraction tower is the key equipment of the solvent extraction process, and its throughput and efficiency determine the scale and size of the entire process equipment. The extraction tower of solvent extraction is divided into several areas, each area has its specific function, and the lower part is generally used as a settling area for heavy components; near the solvent inlet is the asphalt coagulation and washing area, where fresh solvent is injected to wash the condensed recombination to further separate the oil adsorbed on the heavy component; the required oil is dissolved in the interval between the solvent and the inlet of the raw material residue, and the heavy component rich in asphaltene or colloid is separated out; the oil above the inlet of the raw material oil Part of it is the purification area of deasphalting oil, which shows the effect of a selective solvent, and further removes the non-ideal components that have been dissolved in the deasphalting solution to ensure the quality of deasphalting oil. In the existing solvent extraction process, the raw oil is generally fed into the extraction tower from a fixed position in the middle and upper part of the tower, and the quality of the deasphalted oil is adjusted by adopting a one-stage or two-stage process. However, this approach is not based on the properties of the raw material being processed.
当抽提原料性质偏轻时，由于渣油中大部分烃类溶解于溶剂中，形成密度较小的轻相，而另一部分不溶于溶剂的胶质、沥青质，形成密度较大的重相。溶剂抽提过程大部分可溶组分进入抽提塔顶部的回流段，采用这种方式并没有依据加工的原料的特性。When the nature of the extraction raw material is relatively light, because most of the hydrocarbons in the residual oil dissolve in the solvent, a light phase with a low density is formed, while the other part of the colloid and asphaltene, which are insoluble in the solvent, form a heavy phase with a high density . Most of the soluble components in the solvent extraction process enter the reflux section at the top of the extraction column. This method is not based on the characteristics of the raw material being processed.
渣油经过固定床渣油加氢装置以后，加氢渣油中的氢含量提高；饱和分增加；各种金属含量均有所下降；元素硫、氮含量下降，加氢渣油进入催化裂化装置。随着炼厂加工原油的进一步重质化和劣质化，渣油固定床渣油加氢装置得到的加氢渣油中仍含相当一部分较重的胶质、沥青质组分，这些组分常常导致后续催化裂化加工过程中出现加工困难、操作周期变短的问题。利用溶剂脱沥青工艺选择性的除去渣油中最难转化的沥青质和金属化合物，能够得到后续加工所需要的脱沥青油。但是，当溶剂脱沥青原料较轻时，原料中的轻质组分易造成溶剂污染，导致萃取效率降低，萃取油质量变差。After the residual oil passes through the fixed bed residual oil hydrogenation unit, the hydrogen content in the hydrogenated residual oil increases; the saturated content increases; the content of various metals decreases; the content of elemental sulfur and nitrogen decreases, and the hydrogenated residual oil enters the catalytic cracking unit . With the further heavy and inferior quality of crude oil processed by the refinery, the hydrogenated residue obtained from the residual oil fixed bed hydrogenation unit still contains a considerable part of the heavier colloid and asphaltene components, which often This leads to the problems of processing difficulty and shortened operation period in the subsequent catalytic cracking process. The solvent deasphalting process is used to selectively remove the most difficult-to-convert asphaltene and metal compounds in the residual oil, and the deasphalted oil required for subsequent processing can be obtained. However, when the solvent deasphalting raw material is light, the light components in the raw material are likely to cause solvent pollution, resulting in reduced extraction efficiency and poor quality of extracted oil.
发明内容Contents of the invention
本发明的目的是克服萃取效率较低的缺陷，提供一种萃取效率较高的处理重质油的方法。The purpose of the present invention is to overcome the defect of low extraction efficiency and provide a method for processing heavy oil with high extraction efficiency.
本发明的发明人发现，如果在萃取塔的不同高度处通入独立的常规渣油和加氢渣油，能够提高萃取效率，由此得到了本发明。The inventors of the present invention found that if separate conventional residues and hydrogenated residues are introduced at different heights of the extraction tower, the extraction efficiency can be improved, thus obtaining the present invention.
为了实现上述目的，本发明提供了一种处理重质油的方法，所述重质油包括独立的在20℃下的密度为0.934-0.9995g/mL的常规渣油和在20℃下的密度为0.9-0.9335g/mL的加氢渣油，该方法包括将萃取溶剂通入萃取塔的下部，将所述重质油通入所述萃取塔的中上部，使所述重质油与上行的所述萃取溶剂逆流接触进行萃取；将所述常规渣油和所述加氢渣油分别通入所述萃取塔，且在所述萃取塔上，所述常规渣油的进料口高于所述加氢渣油的进料口。In order to achieve the above object, the present invention provides a method for processing heavy oil, which includes conventional residual oil with a density of 0.934-0.9995 g/mL at 20°C and a density at 20°C It is 0.9-0.9335g/mL hydrogenated residual oil, the method comprises that the extraction solvent is passed into the lower part of the extraction tower, and the heavy oil is passed into the middle and upper part of the extraction tower, so that the heavy oil and the uplink The extraction solvent is countercurrently contacted for extraction; the conventional residual oil and the hydrogenated residual oil are respectively passed into the extraction tower, and on the extraction tower, the feed inlet of the conventional residual oil is higher than The feed port of the hydrogenated residual oil.
通过上述技术方案，本发明能够有效地提高处理重质油的萃取效率。采用这种方式，能够将炼厂固定床渣油加氢装置得到的加氢渣油进行溶剂抽提，得到质量好的脱沥青油进行催化裂化，通过改善催化裂化装置进料，提高催化裂化装置的运行周期。Through the above technical solution, the present invention can effectively improve the extraction efficiency of heavy oil. In this way, the hydrogenated residual oil obtained from the fixed-bed residual oil hydrogenation unit of the refinery can be solvent extracted to obtain good-quality deasphalted oil for catalytic cracking. By improving the feed of the catalytic cracking unit, the catalytic cracking unit can be improved. operating cycle.
本发明的其他特征和优点将在随后的具体实施方式部分予以详细说明。Other features and advantages of the present invention will be described in detail in the following detailed description.
附图说明Description of drawings
附图是用来提供对本发明的进一步理解，并且构成说明书的一部分，与下面的具体实施方式一起用于解释本发明，但并不构成对本发明的限制。在附图中：The accompanying drawings are used to provide a further understanding of the present invention, and constitute a part of the description, together with the following specific embodiments, are used to explain the present invention, but do not constitute a limitation to the present invention. In the attached picture:
图1是本发明特别优选的一种实施方式的所使用的萃取塔的结构示意图。Fig. 1 is a structural schematic diagram of an extraction tower used in a particularly preferred embodiment of the present invention.
附图标记说明Explanation of reference signs
1 第一进料入口 11 第一进料分布器1 First feed inlet 11 First feed distributor
111 第一填料111 First packing
2 第二进料入口 21 第二进料分布器2 Second feed inlet 21 Second feed distributor
211 第二填料211 Second packing
4 萃取物出口 6 萃取塔4 Extract outlet 6 Extraction column
7 萃取溶剂进口 71 萃取溶剂分布器7 Extraction solvent inlet 71 Extraction solvent distributor
8 萃余液出口 9 加热器8 Raffinate outlet 9 Heater
具体实施方式detailed description
以下结合附图对本发明的具体实施方式进行详细说明。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。Specific embodiments of the present invention will be described in detail below in conjunction with the accompanying drawings. It should be understood that the specific embodiments described here are only used to illustrate and explain the present invention, and are not intended to limit the present invention.
在本发明中，在未作相反说明的情况下，使用的方位词如“上、下、底、顶”通常是在本发明提供的装置正常使用的情况下定义的，具体地可参考图1所示的图面方向，“内、外”是指相应轮廓的内和外；使用的液体或气体的体积数值为20℃和1个标准大气压下的数值。In the present invention, under the situation of not stating to the contrary, the orientation words used such as "upper, lower, bottom, top" are generally defined under the normal use of the device provided by the present invention, specifically with reference to Fig. 1 In the direction of the drawing shown, "inside and outside" refer to the inside and outside of the corresponding contour; the volume value of the liquid or gas used is the value at 20°C and 1 standard atmospheric pressure.
本发明提供了一种处理重质油的方法，所述重质油包括独立的在20℃下的密度为0.934-0.9995g/mL的常规渣油和在20℃下的密度为0.9-0.9335g/mL的加氢渣油，该方法包括将萃取溶剂通入萃取塔的下部，将所述重质油通入所述萃取塔的中上部，使所述重质油与上行的所述萃取溶剂逆流接触进行萃取；将所述常规渣油和所述加氢渣油分别独立地通入所述萃取塔，且在所述萃取塔上，所述常规渣油的进料口高于所述加氢渣油的进料口。The present invention provides a method for treating heavy oil, which comprises independent conventional residues having a density of 0.934-0.9995 g/mL at 20°C and a density of 0.9-0.9335 g at 20°C /mL of hydrogenated residual oil, the method comprises that the extraction solvent is passed into the lower part of the extraction tower, the heavy oil is passed into the middle and upper part of the extraction tower, and the heavy oil is mixed with the upward extraction solvent Countercurrent contacting for extraction; the conventional residual oil and the hydrogenated residual oil are independently fed into the extraction tower, and on the extraction tower, the feed inlet of the conventional residual oil is higher than that of the hydrogenated residual oil The feed port of the hydrogen residue.
其中，所述常规渣油与所述加氢渣油的体积比可以在较大范围内变化，例如为1：(0.01-5)。其中，所述常规渣油与所述加氢渣油的体积比是指在单位时间内，通入所述萃取塔的所述常规渣油的体积相对于通入所述萃取塔的所述加氢渣油的体积的比例。Wherein, the volume ratio of the conventional residual oil to the hydrogenated residual oil can vary within a wide range, for example, 1:(0.01-5). Wherein, the volume ratio of the conventional residue to the hydrogenated residue refers to the volume of the conventional residue passed into the extraction tower relative to the volume of the hydrogenated residue passed into the extraction tower within a unit time. The ratio of the volume of the hydrogen residue.
其中，根据本发明一种优选的实施方式，在单位时间内，通入所述萃取塔6的所述常规渣油与所述加氢渣油的体积比为1：(0.1-3)；更优选为1：(0.3-2)。Wherein, according to a preferred embodiment of the present invention, within a unit time, the volume ratio of the conventional residual oil and the hydrogenated residual oil passed into the extraction tower 6 is 1: (0.1-3); Preferably it is 1:(0.3-2).
其中，在所述萃取塔上，所述常规渣油的进料口高于所述加氢渣油的进料口即可，即，所述常规渣油的进料口与所述萃取溶剂的进料口之间的高度差大于所述加氢渣油的进料口与所述萃取溶剂的进料口之间的高度差即可，例如所述常规渣油的进料口与所述萃取溶剂的进料口之间的高度差相对于所述加氢渣油的进料口与所述萃取溶剂的进料口之间的高度差的比例可以为(1.02-1.5)：1，优选为(1.05-1.3)：1。Wherein, on the extraction tower, the feed inlet of the conventional residue oil is higher than the feed inlet of the hydrogenated residue oil, that is, the feed inlet of the conventional residue oil and the extraction solvent It is sufficient that the height difference between the feed ports is greater than the height difference between the feed port of the hydrogenated residue and the feed port of the extraction solvent, for example, the feed port of the conventional residue and the extraction solvent The ratio of the height difference between the feed ports of the solvent to the height difference between the feed ports of the hydrogenated residue and the extraction solvent can be (1.02-1.5): 1, preferably (1.05-1.3):1.
所述萃取温度可以根据所用的溶剂进行改变，例如可以为40-290℃，优选为60-270℃。特别优选地；所述萃取塔的塔底温度为50-185℃，塔顶温度为60-195℃。所述塔底温度低于所述塔顶温度。The extraction temperature can be changed according to the solvent used, for example, it can be 40-290°C, preferably 60-270°C. Particularly preferably; the temperature at the bottom of the extraction tower is 50-185°C, and the temperature at the top of the tower is 60-195°C. The bottom temperature is lower than the top temperature.
其中，所述萃取塔的压力可以根据所用的溶剂进行改变，例如，所述萃取塔的压力可以为1-7MPa，优选为2-6MPa。Wherein, the pressure of the extraction tower can be changed according to the solvent used, for example, the pressure of the extraction tower can be 1-7MPa, preferably 2-6MPa.
其中，所述萃取溶剂的体积与所述常规渣油和所述加氢渣油的总体积的比例可以在较大范围内变化，例如可以为(0.5-20)：1，优选为(1-15)：1；更优选为(2-10)：1。通入所述萃取塔的萃取溶剂的总体积与所述常规渣油和所述加氢渣油的总体积的比例可以称为溶剂比。Wherein, the ratio of the volume of the extraction solvent to the total volume of the conventional residual oil and the hydrogenated residual oil can vary within a wide range, for example, it can be (0.5-20): 1, preferably (1- 15):1; more preferably (2-10):1. The ratio of the total volume of the extraction solvent passed into the extraction column to the total volume of the conventional residue and the hydrogenated residue may be referred to as a solvent ratio.
其中，所述萃取溶剂可以含有具有2-8个碳原子的烃。例如，所述萃取溶剂包括但不限于乙烷、丙烷、丙烯、正丁烷、异丁烷、正戊烷、异戊烷、己烷、庚烷和辛烷中的至少一种。优选所述萃取溶剂包括C3的烷烃、C3的烯烃、C4的烷烃、C4的烯烃、C5的烷烃和C5的烯烃中的至少一种。例如所述萃取溶剂含有40-50体积％的正丁烷和50-60体积％的异丁烯。Wherein, the extraction solvent may contain hydrocarbons having 2-8 carbon atoms. For example, the extraction solvent includes but is not limited to at least one of ethane, propane, propylene, n-butane, isobutane, n-pentane, isopentane, hexane, heptane and octane. Preferably, the extraction solvent includes at least one of C3 alkanes, C3 alkenes, C4 alkanes, C4 alkenes, C5 alkanes and C5 alkenes. For example, the extraction solvent contains 40-50% by volume of n-butane and 50-60% by volume of isobutene.
其中，根据本发明的方法，将萃取溶剂通入萃取塔的下部，即可以将全部萃取溶剂通入所述萃取塔的下部，也可以将萃取溶剂中的一部分通入所述萃取塔的下部，将萃取溶剂中的另一部分通入所述萃取塔的中上部，例如将萃取溶剂中的另一部分与所述常规渣油混合后经所述常规渣油的进料口通入所述萃取塔。Wherein, according to the method of the present invention, the extraction solvent is passed into the bottom of the extraction tower, that is, all the extraction solvent can be passed into the bottom of the extraction tower, or a part of the extraction solvent can be passed into the bottom of the extraction tower, Another part of the extraction solvent is passed into the middle and upper part of the extraction tower, for example, another part of the extraction solvent is mixed with the conventional residue and then passed into the extraction tower through the feed port of the conventional residue.
其中，根据本发明的一种优选实施方式，所述常规渣油包括减压渣油、常压渣油和减粘裂化渣油中的至少一种，所述萃取溶剂包括第一萃取溶剂和第二萃取溶剂，所述第一萃取溶剂通入萃取塔的下部；所述第二萃取溶剂与所述常规渣油混合后经所述常规渣油的进料口通入所述萃取塔。所述第二萃取溶剂与所述常规渣油混合能够起到预混的作用。所述第二萃取溶剂与所述常规渣油的混合可以通过静态混合器进行。在该优选实施方式中，在通入所述萃取塔的萃取溶剂总量不变的情况下，将通入所述萃取塔的萃取溶剂分为第一萃取溶剂和第二萃取溶剂，分别通入萃取塔的下部和与所述常规渣油混合经所述常规渣油的进料口通入，能够进一步提高萃取效率。Wherein, according to a preferred embodiment of the present invention, the conventional residue includes at least one of vacuum residue, atmospheric residue, and visbroken residue, and the extraction solvent includes the first extraction solvent and the second extraction solvent. Two extraction solvents, the first extraction solvent is passed into the lower part of the extraction tower; the second extraction solvent is mixed with the conventional residual oil and then passed into the extraction tower through the feed port of the conventional residual oil. The mixing of the second extraction solvent with the conventional resid can function as a premix. The mixing of the second extraction solvent and the conventional resid may be performed by a static mixer. In this preferred embodiment, under the condition that the total amount of the extraction solvent passed into the extraction tower remains unchanged, the extraction solvent passed into the extraction tower is divided into a first extraction solvent and a second extraction solvent, which are respectively fed into The lower part of the extraction tower is mixed with the conventional residual oil and fed through the feed port of the conventional residual oil, which can further improve the extraction efficiency.
其中，所述第一萃取溶剂与所述第二萃取溶剂的体积比可以为(0.1-1)：1，优选为(0.2-5)：1。Wherein, the volume ratio of the first extraction solvent to the second extraction solvent may be (0.1-1):1, preferably (0.2-5):1.
其中，所述第一萃取溶剂与所述第二萃取溶剂的组成可以相同或不同，优选所述第一萃取溶剂与所述第二萃取溶剂的组成相同。Wherein, the composition of the first extraction solvent and the second extraction solvent may be the same or different, preferably the composition of the first extraction solvent and the second extraction solvent are the same.
本发明中，所述常规渣油可以包括常压渣油和/或减压渣油；所述常压渣油可以为石油原油经常压分馏后剩余的沸程大于350℃的馏分；所述减压渣油可以为减压渣油经减压分馏后剩余的沸程大于500℃的馏分；所述加氢渣油可以为渣油经过固定床加氢后得到的加氢产物经常压分馏后剩余的沸程大于350℃的馏分。In the present invention, the conventional residual oil may include atmospheric residual oil and/or vacuum residual oil; the atmospheric residual oil may be a fraction with a boiling range greater than 350°C remaining after the atmospheric pressure fractionation of petroleum crude oil; The pressure residue can be the fraction with a boiling range greater than 500°C remaining after the vacuum residue is subjected to vacuum fractionation; the hydrogenated residue can be the hydrogenation product obtained after the residue is hydrogenated in a fixed bed and remains after normal pressure fractionation. The fraction whose boiling range is greater than 350°C.
参考图1，说明本发明特别优选的一种实施方式；本发明的方法包括将所述重质油通入萃取塔6中进行萃取；该萃取塔包括萃取塔6以及从上到下依次设置且与所述萃取塔连通的至少一个萃取物出口4、至少一个萃取溶剂进口7和至少一个萃余液出口8；在所述萃取物出口4和所述萃取溶剂进口7之间，设置有至少两个进料入口，所述至少两个进料入口包括第一进料入口1和第二进料入口2；且所述第一进料入口1与同一个所述萃取溶剂进口7之间的高度差大于所述第二进料入口2与同一个所述萃取溶剂进口7之间的高度差；将所述常规渣油通入第一进料入口1，将所述加氢渣油通入所述第二进料入口2。其中，所述第一进料入口1与同一个所述萃取溶剂进口7之间的高度差大于所述第二进料入口2与同一个所述萃取溶剂进口7之间的高度差即可，例如所述第一进料入口1与同一个所述萃取溶剂进口7之间的高度差相对于所述第二进料入口2与同一个所述萃取溶剂进口7之间的高度差的比例可以为(1.02-1.5)：1，优选为(1.05-1.3)：1。其中，所述萃取塔6可以为逆流萃取塔；所述萃取塔6的塔高和塔径可以为溶剂脱沥青领域常规的选择，例如塔高可以为15-40米，塔径可以为1-5米。其中，优选地，萃取溶剂进口7还连接有置于萃取塔6内的萃取溶剂分布器71；萃取溶剂可以经萃取溶剂分布器71得到分布。其中，所述第一进料入口1上可以连接有第一进料分布器11；所述第二进料入口2上可以连接有第二进料分布器21；所述第一进料入口1和所述第二进料入口2之间可以设置有筛板、转盘和填料中的至少一种。筛板、转盘和填料的选择和设置方式可以为本领域常规的选择，本领域技术人员对此十分熟知，本发明在此不再赘述。With reference to Fig. 1, illustrate a kind of embodiment that the present invention is particularly preferred; The method of the present invention comprises that described heavy oil is passed in extraction tower 6 and extracts; This extraction tower comprises extraction tower 6 and arranges successively from top to bottom and At least one extract outlet 4, at least one extraction solvent inlet 7 and at least one raffinate outlet 8 communicated with the extraction tower; between the extract outlet 4 and the extraction solvent inlet 7, at least two feed inlet, the at least two feed inlets include the first feed inlet 1 and the second feed inlet 2; and the height between the first feed inlet 1 and the same extraction solvent inlet 7 The difference is greater than the height difference between the second feed inlet 2 and the same extraction solvent inlet 7; the conventional residue is passed into the first feed inlet 1, and the hydrogenated residue is passed into the Describe the second feed inlet 2. Wherein, it is sufficient that the height difference between the first feed inlet 1 and the same extraction solvent inlet 7 is greater than the height difference between the second feed inlet 2 and the same extraction solvent inlet 7, For example, the ratio of the height difference between the first feed inlet 1 and the same extraction solvent inlet 7 to the height difference between the second feed inlet 2 and the same extraction solvent inlet 7 can be It is (1.02-1.5):1, preferably (1.05-1.3):1. Wherein, the extraction tower 6 can be a countercurrent extraction tower; the tower height and the tower diameter of the extraction tower 6 can be conventional selections in the field of solvent deasphalting, for example, the tower height can be 15-40 meters, and the tower diameter can be 1-40 meters. 5 meters. Wherein, preferably, the extraction solvent inlet 7 is also connected with an extraction solvent distributor 71 placed in the extraction tower 6 ; the extraction solvent can be distributed through the extraction solvent distributor 71 . Wherein, the first feed inlet 1 may be connected with a first feed distributor 11; the second feed inlet 2 may be connected with a second feed distributor 21; the first feed inlet 1 At least one of a sieve plate, a turntable and a filler may be arranged between the second feed inlet 2 . The selection and arrangement of the sieve plate, turntable and packing can be conventional selections in the field, which are well known to those skilled in the art, and the present invention will not repeat them here.
实施例1Example 1
本实施例举例说明对包括所述常规渣油(减压渣油)与所述加氢渣油的重质油进行处理的方法。按照国家和行业标准检测所述常规渣油与所述加氢渣油的性质，结果如表1所示。This example illustrates a process for the treatment of heavy oils including the conventional residue (vacuum residue) and the hydrogenated residue. The properties of the conventional residue and the hydrogenated residue were detected according to national and industry standards, and the results are shown in Table 1.
表1Table 1
参考图1，设置萃取塔，该萃取塔包括萃取塔6以及从上到下依次设置且与所述萃取塔连通的萃取物出口4、第一进料入口1、第二进料入口2、萃取溶剂进口7和萃余液出口8，第一进料入口1与萃取溶剂进口7之间的高度差相对于第二进料入口2与萃取溶剂进口7之间的高度差的比例为1.15：1。第一进料入口1与置于萃取塔内的第一进料分布器11连接；第二进料入口2与置于萃取塔内的第一进料分布器21连接；在萃取塔内，第一进料入口1与第二进料入口2之间设置有第一填料111；第二进料入口2与萃取溶剂进口7之间设置有第二填料211；如上所述的填料均为规整填料。With reference to Fig. 1, extracting tower is set, and this extracting tower comprises extracting tower 6 and is arranged successively from top to bottom and extract outlet 4 that is communicated with described extracting tower, the first feed inlet 1, the second feed inlet 2, extraction Solvent inlet 7 and raffinate outlet 8, the ratio of the height difference between the first feed inlet 1 and the extraction solvent inlet 7 to the height difference between the second feed inlet 2 and the extraction solvent inlet 7 is 1.15:1 . The first feed inlet 1 is connected with the first feed distributor 11 placed in the extraction tower; the second feed inlet 2 is connected with the first feed distributor 21 placed in the extraction tower; in the extraction tower, the first A first packing 111 is arranged between the feed inlet 1 and the second feed inlet 2; a second packing 211 is arranged between the second feed inlet 2 and the extraction solvent inlet 7; the above-mentioned packings are structured packings .
参考图1，将常规渣油通入第一进料入口1，将加氢渣油通入所述第二进料入口2，其中，萃取塔中的压力为5.0MPa，总溶剂比为5：1，其中总溶剂比是指在单位时间内，通入萃取塔的溶剂的体积相对于常规渣油和加氢渣油的总体积的比例；在单位时间内，通入萃取塔常规渣油和加氢渣油的体积的比例为1：0.5。萃取溶剂含有84.6体积％的正丁烷、13.4体积％的异丁烯。萃取塔的塔底温度为115℃，塔顶温度为130℃。将萃取溶剂全部经萃取溶剂进口7导入。从萃取物出口4导出萃取物，从萃余液出口8导出萃余液。With reference to Fig. 1, conventional residue oil is passed into first feed inlet 1, and hydrogenated residue oil is passed into described second feed inlet 2, wherein, the pressure in the extraction tower is 5.0MPa, and total solvent ratio is 5: 1, where the total solvent ratio refers to the ratio of the volume of the solvent that passes into the extraction tower relative to the total volume of conventional residue and hydrogenated residue in unit time; The volume ratio of hydrogenated residue is 1:0.5. The extraction solvent contained 84.6% by volume of n-butane and 13.4% by volume of isobutene. The temperature at the bottom of the extraction tower was 115°C, and the temperature at the top of the tower was 130°C. All the extraction solvents are introduced through the extraction solvent inlet 7. The extract is taken out from the extract outlet 4 and the raffinate is taken out from the raffinate outlet 8 .
对比例1Comparative example 1
使用实施例1中所述的萃取塔进行萃取，不同的是，封闭第一进料入口1，将常规渣油和加氢渣油按照1：0.5的比例混合后，经过第二进料入口2导入萃取塔6。Use the extraction tower described in Example 1 for extraction, the difference is that the first feed inlet 1 is closed, the conventional residue and the hydrogenated residue are mixed in a ratio of 1:0.5, and then pass through the second feed inlet 2 Import extraction tower 6.
对比例2Comparative example 2
使用实施例1中所述的萃取塔进行萃取，不同的是，封闭第二进料入口2，将常规渣油和加氢渣油按照1：0.5的比例混合后，经过第一进料入口1导入萃取塔6。Use the extraction tower described in Example 1 for extraction, the difference is that the second feed inlet 2 is closed, the conventional residue and the hydrogenated residue are mixed in a ratio of 1:0.5, and then pass through the first feed inlet 1 Import extraction tower 6.
测试实施例1Test Example 1
按照国家或者行业标准中的方法，测定实施例1和对比例1、2得到萃取物去除萃取溶剂后的产物的性质，结果如表2所示。According to the method in the national or industry standard, the properties of the product after removing the extraction solvent from the extract obtained in Example 1 and Comparative Examples 1 and 2 were measured, and the results are shown in Table 2.
表2Table 2
根据表2的数据可见，本发明提供的萃取塔和方法能够显著地提高萃取重质油的效率。According to the data in Table 2, it can be seen that the extraction tower and method provided by the present invention can significantly improve the efficiency of extracting heavy oil.
以上结合附图详细描述了本发明的优选实施方式，但是，本发明并不限于上述实施方式中的具体细节，在本发明的技术构思范围内，可以对本发明的技术方案进行多种简单变型，这些简单变型均属于本发明的保护范围。The preferred embodiment of the present invention has been described in detail above in conjunction with the accompanying drawings, but the present invention is not limited to the specific details of the above embodiment, within the scope of the technical concept of the present invention, various simple modifications can be made to the technical solution of the present invention, These simple modifications all belong to the protection scope of the present invention.
另外需要说明的是，在上述具体实施方式中所描述的各个具体技术特征，在不矛盾的情况下，可以通过任何合适的方式进行组合，为了避免不必要的重复，本发明对各种可能的组合方式不再另行说明。In addition, it should be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable way if there is no contradiction. The combination method will not be described separately.
此外，本发明的各种不同的实施方式之间也可以进行任意组合，只要其不违背本发明的思想，其同样应当视为本发明所公开的内容。In addition, various combinations of different embodiments of the present invention can also be combined arbitrarily, as long as they do not violate the idea of the present invention, they should also be regarded as the disclosed content of the present invention.
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410568037.4ACN105524646B (en) | 2014-10-22 | 2014-10-22 | Method for extracting and processing solvent of residual oil |
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410568037.4ACN105524646B (en) | 2014-10-22 | 2014-10-22 | Method for extracting and processing solvent of residual oil |
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| CN105524646A CN105524646A (en) | 2016-04-27 |
| CN105524646Btrue CN105524646B (en) | 2017-05-24 |
| Application Number | Title | Priority Date | Filing Date |
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| CN201410568037.4AActiveCN105524646B (en) | 2014-10-22 | 2014-10-22 | Method for extracting and processing solvent of residual oil |
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| CN118792079B (en)* | 2023-04-13 | 2025-08-12 | 中国石油化工股份有限公司 | Processing method and processing device for low-sulfur ship combustion in residual oil production |
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