JPH0115558B2 - - Google Patents

Description

[Detailed description of the invention]

[Technical Field of the Invention] The present invention relates to a method for producing raw material oil for gasoline production, and more specifically, the present invention relates to a method for producing raw material oil for gasoline production. Relating to a method for manufacturing. [Background of the Invention] In recent years, from the viewpoint of effective utilization of petroleum resources, various studies have been conducted on methods for reforming heavy petroleum residues. In general, when preparing raw material oil for gasoline production from heavy oil, it is difficult to effectively remove impurities such as asphaltene and metal components in the heavy oil.
is an important issue. Asphaltenes and heavy metals present in feedstock oil become harmful components in subsequent refining processes such as catalytic cracking, and especially Ni, Fe,
Metals such as V promote coking of the catalytic cracking catalyst and reduce the catalytic activity, resulting in a decrease in the liquid yield of gasoline. Conventionally, the main methods for demetallizing and removing asphaltenes from heavy oil include (a) separating asphaltenes by contacting the heavy oil with a low-boiling point paraffinic hydrocarbon such as propane or an organic solvent such as benzene or toluene; Solvent deasphalting method to remove (for example, JP-A-59-
Publication No. 27985, Publication No. 57-31989, Publication No. 53-54205
No. 59-41389, etc.), (b) a method using a specific solid catalyst (for example, JP-A No. 52-117905),
No. 54-113602, etc.), (c) Mixing two or more types of heavy oils with different properties such as history and aroma, such as coal tar and petroleum heavy oil, heating and cooling. Batch method in which insoluble substances that are harmful impurities in heavy oil are deposited and removed through a process (for example, Japanese Patent Publication No. 49-26481,
JP-A-49-11603, etc.) are known. However, in the method (a) above that uses a solvent, the manufacturing process becomes complicated because a solvent separation and recovery process is required, and manufacturing conditions such as selecting a solvent and setting deasphalting conditions are required. It is not always easy to select the optimum one, and furthermore, there is a drawback that the manufacturing cost increases. Also, in the method using the catalyst described in (b) above,
Similarly, selection of catalyst, maintenance and regeneration of catalyst activity,
Furthermore, there are problems such as complicated steps such as removal of the deactivated catalyst and increased manufacturing costs, which are disadvantageous from a technical and economic point of view. Furthermore, in the method (c) above, the production of insoluble substances and their removal are performed by stationary cooling, stationary sedimentation separation, centrifugation, etc., and batch operations are required in either case. However, as is well known, batch operations are disadvantageous in that productivity is poor and quality varies from batch to batch. [Summary of the Invention] The present invention has been made in view of the drawbacks of the above-mentioned prior art, and aims to efficiently convert raw material oil for gasoline production by effectively removing metals and asphaltene from heavy oil. and to provide a method for continuous preparation. The present inventors focused on the fact that most of the metal components that become obstacles in the catalytic cracking process etc. are concentrated in the insoluble substances produced by mixing two or more types of heavy oil. As a result of trying various methods to efficiently separate and remove insoluble substances, we have found that the flow of a heavy oil mixture prepared at a high temperature is brought into contact with or collides with the product raw material oil that has been partially extracted and circulated. It has been found that rapid cooling of a quality oil mixture promotes the formation and aggregation of insoluble substances, thereby effectively achieving demetallization and asphaltene removal through continuous operation. The present invention has been made based on the above findings. That is, the continuous production method of raw material oil for gasoline production of the present invention involves preparing a high-temperature heavy oil mixture consisting of at least two kinds of heavy oils, and further cooling this mixture to remove insoluble substances in the heavy oil mixture. When continuously producing raw material for gasoline production by producing substances and removing the insoluble substances from the heavy oil mixture, a part of the produced raw material for gasoline production is extracted and circulated to the cooling step. The heavy oil mixture is cooled by bringing the circulating oil flow into contact with the high temperature heavy oil mixture flow. FIG. 1 is a process chart showing an overview of the method of the present invention. As shown in FIG. 1, in the method of the present invention,
First, a high-temperature 200 ml of heavy oil consisting of at least two types of heavy oil selected from petroleum-based ordinary pressure or vacuum direct distillation residue oil, coal tar, petroleum-based naphtha cracking residue oil, thermal cracking residue oil, hydrocracking residue oil, etc. Prepare a heavy oil mixture at ~390 °C. Preparation of this high-temperature heavy oil mixture is preferably carried out by heating each of the component heavy oils in advance and then combining them (line blending); however, after mixing the component heavy oils, Alternatively, it may be carried out by heating while mixing. The hot heavy oil mixture is then cooled to a temperature below 100° C. to form insoluble materials in the heavy oil mixture. In the method of the present invention, this cooling step is carried out by extracting a part of the already produced raw material oil for gasoline production and using it as circulating oil, and bringing the flow of this circulating oil into contact with the flow of the high-temperature heavy oil mixture. conduct. The circulating oil needs to be cooled to 50 to 80°C before it comes into contact with the high-temperature heavy oil mixture, but the circulating oil naturally cools down to the above temperature range while moving through the circulation path. In some cases, forced cooling is not necessarily necessary. It should be noted that if the temperature of the circulating oil is about 50° C. or lower, the fluidity will generally decrease, which is not preferable. The cooling step is preferably carried out by bringing the jet of the high-temperature heavy oil mixture and the jet of the circulating oil into countercurrent contact or collision. In this way, the high-temperature heavy oil mixture is rapidly cooled by the collision movement of the circulating oil and the heavy oil mixture, and the temperature conditions necessary for the generation of insoluble substances are satisfied, and the collision of the precipitated insolubles is prevented. Therefore, aggregation of insoluble matter is promoted. On the other hand, the insoluble substances precipitated and aggregated in this manner are successively separated and removed, and continuous preparation of raw material oil for gasoline production is achieved. [Specific Description of the Invention] Hereinafter, the method of the present invention will be explained in more detail based on preferred specific examples thereof. FIG. 2 is a layout diagram of the main parts of an apparatus used to carry out the method of the present invention, and FIG. 3 is an overall layout diagram including the main parts shown in FIG. As shown in FIGS. 2 and 3, the apparatus for carrying out the method of the present invention comprises an upper tank 1 and a lower tank 2 having substantially the same diameter and arranged substantially vertically. 1/2 to 1/10 preferably 1/5 to 1/ of the diameter of
They are connected by a relatively small cylindrical tube 3 having a diameter of 6. A single heavy oil introduction pipe 4 is introduced into the lower tank 2 by penetrating its side wall, and its downstream end opens upward toward the cylindrical pipe 3 within the lower tank 2.
Further, the upstream side of the introduction pipe 4 branches relatively close to the lower tank 2 into introduction pipes 4a and 4b for the raw material heavy oil, and these introduction pipes 4a and 4b are connected to heaters 5a and 5b, respectively. , the raw material heavy oil tank 7 via the pump 6a or 6b.
It is bonded to a or 7b. Further, a heavy liquid extraction pipe 8 is connected to the bottom of the lower tank 2, and this extraction pipe 8 is connected to a heavy liquid tank 10 via a pump 9. On the other hand, a light liquid extraction pipe 11 is connected to the upper part of the upper tank 1, and this extraction pipe 11 is connected to a product oil tank 14 via a receiving tank 12 and a pump 13. Further, a circulation pipe 15 is branched and connected downstream of the pump 13 of the extraction pipe 11.
5 extends into the upper tank 1 and opens downward toward the cylindrical pipe 3 within the upper tank 1. A cooler 16 is disposed in the middle of this circulation pipe 15. Also upper tank 1
Inside, from one side wall to the opposite side wall,
A plurality of substantially horizontal shelves 17 extend, the lower ones of which extend beyond the center of the tank 1 toward the opposite side walls. Moreover, heaters 20a and 20b are arranged around the bottoms of the tanks 1 and 2. Next, a typical embodiment of preparing raw material oil for gasoline production using the above-mentioned apparatus will be described.
In the following description, "parts" and "%" are based on weight unless otherwise specified. First, heavy oil A with relatively low aroma is pumped from tank 7a, and heavy oil B with relatively high aroma is pumped from tank 7b with pump 6a or 6b, respectively.
200 to 390 by heater 5a or 5b.
After heating to ℃, the two liquids are mixed just before the lower tank 2, and the two liquids are mixed through the introduction pipe 4 into the lower tank 2.
It flows out or spouts directly below the inner cylindrical pipe 3. The heavy oil A is, for example, petroleum-based normal pressure or vacuum direct distillation residue oil, and the heavy oil B is, for example,
Coal tar, petroleum naphtha cracking residue oil, thermal cracking residue oil, hydrocracking residue oil, etc. are used. It is preferable to use the heavy oil B in an amount of 30 to 70 parts per 100 parts of the mixed oil in consideration of the removal efficiency of insoluble substances and the properties of the product raw material oil. The introduced high-temperature heavy oil mixture mainly rises through the cylindrical pipe 3 and passes through the circulation pipe 15 and the cooler 1.
By contact or collision with the circulating light liquid (50 to 90°C) flowing out through 6, it is preferably cooled to below 100°C, and the insoluble substances generated by this series of mixing and cooling are promoted to flocculate and settle. ,
It flows down through the cylindrical pipe 3 in contact with the heavy oil mixture and is deposited at the bottom of the lower tank 2. The heavy liquid, which mainly consists of deposited insoluble substances, is heated by the heater 20b and flows into the bottom pipe 8 while maintaining its fluidity.
is extracted from the heavy liquid tank 10 via a pump 9.
will be put on hold. On the other hand, the light liquid from which insoluble substances have been removed in the upper tank 1 further passes between the shelves 17 and rises, further separating the insoluble substances, and is extracted from the upper part of the upper tank 1 through the piping 11, and is then drawn out from the upper tank 1 through the pipe 11, The product oil is stored in a product oil tank 14 via a pump 13. Further, a part of the light liquid coming out of the pump 13 is circulated to the upper tank 1 via the piping 15, and is made to flow out under the shelf plate 17 in the upper tank 1. In the above, a preferred example of the method of the present invention and its operation mode have been explained based on a specific apparatus. However, it will be readily apparent to those skilled in the art that various modifications to the above example method may be made within the scope of the present invention. For example, the raw material heavy oil is not limited to two types, but three or more types can be used. Furthermore, it is preferable that the introduction pipe 4 for the raw material heavy oil is extended into the lower tank 2 and opened directly below the cylindrical pipe 3, but the invention is not limited thereto. is obtained. The introduction pipe 4 is not limited to a single pipe, but a plurality of introduction pipes can be connected to the lower tank 2 or extended into the lower tank 2 for each raw material heavy oil. Furthermore, although the shelf board 17 in the upper tank 1 has the effect of promoting separation of the light liquid and insoluble substances, it may be tilted diagonally downward in order to prevent the insoluble substances from depositing on the shelf board 17. preferable. In the above example, the volumes of the upper tank 1 and the lower tank 2 are approximately the same, but the ratio can be changed as appropriate in consideration of mixing and separation. According to the method described above, raw oils are mixed in pipes at high temperatures (line blending),
Furthermore, since the cooling and deposition can be carried out in a tank with a relatively large capacity, there is no problem of clogging of piping by insoluble substances produced. Furthermore, by circulating a portion of the product light liquid, etc., a temperature difference necessary for mixing and separation is provided, and these temperatures can be easily set and controlled. EXAMPLES OF THE INVENTION The following is an example of the actual operation of an example of an apparatus used in the method of the invention essentially shown in FIGS. 2 and 3. Although the following examples are relatively small-scale examples, they are believed to provide a sufficient understanding of the effectiveness of the method of the present invention. Raw material oil for gasoline production was produced using petroleum-based heavy oil A, ethylene tar petroleum cracking heavy oil B, and coal-based heavy oil C having properties shown in Table 1 below as raw material heavy oils. Example 1 Heavy oil A was fed at a rate of 140 g/min and heavy oil B at a rate of 60 g/min from feed pumps 6a and 6b, heated to 200°C by heaters 5a and 5b, respectively, and then pipes 4a, From 4b to lower tank 2 (diameter approx. 250mm, 40
) and flowed out from a position 100 mm directly below the lower end of the cylindrical pipe 3 (diameter approximately 50 mm, length 200 mm) in the lower tank 2. The blending ratio of heavy oil A and heavy oil B was A:B=70:30. On the other hand, under the shelf of the upper tank 1 (about 300 mm in diameter) equipped with shelf boards 17 (total of 5) as shown, piping 15,
The light liquid at a temperature of about 80°C was circulated through the cooler 16 at a rate of 1/min and contacted with the jet of the heavy oil mixture to rapidly cool the heavy oil mixture to a temperature below 100°C. The light liquid extracted from the upper tank 1 is collected at a rate of 166 g/min (yield 83%) in the storage tank 14, while it is heated to about 200°C and flows from the bottom pipe 8 of the lower tank 2. A heavy liquid, consisting mainly of insoluble materials, was recovered. The metal content and properties of the recovered light liquid and heavy liquid were as shown in Table 1. Example 2 Using heavy oil A and heavy oil C, light liquid and heavy liquid were recovered from a heavy oil mixture in the same manner and under the same conditions as in Example 1 above, and their metal content and properties were analyzed. The analysis results were as shown in Table 1. Comparative Example Heavy oil A was deasphalted by a solvent deasphalting method using Normanheptane as a solvent according to a conventional method,
The metal content and properties of the obtained light liquid were analyzed. The analysis results were as shown in Table 1. As is clear from the above analysis results, the light liquids obtained in Example 1 and Example 2 according to the method of the present invention have superior metal removal effects compared to the comparative example, and in particular,
To promote coking in the catalytic cracking process,
It can be seen that the Ni component, which causes a decrease in catalyst activity, is removed extremely effectively.

〔Effect of the invention〕

As described above, according to the present invention, two or more types of heavy oils are mixed and the resulting insoluble substances containing metal components are separated and removed to continuously prepare feedstock oil suitable for gasoline production. According to this method, the following excellent effects can be obtained. (b) Unlike conventional methods, there is no need to use any solvent or catalyst as a means of demetallization or asphaltene removal, so the manufacturing process is simplified, and manufacturing conditions can be easily set and controlled; It is technically superior and economically advantageous. (b) Metal components and asphaltenes in heavy oil can be efficiently removed through a series of continuous operations, which is advantageous in terms of productivity compared to conventional batch processes, and Since problems such as changes in quality are resolved, it is also excellent in terms of quality stability and reliability. (c) Since a part of the product oil is circulated so that it comes into fluid contact with the flow of the heavy oil mixture, the temperature conditions necessary for the generation of insoluble substances due to the collision motion between the circulating oil and the heavy oil mixture is satisfied (cooling effect), precipitation and collision of insoluble substances,
A synergistic effect of promoting aggregation is exerted.

[Brief explanation of drawings]

FIG. 1 is a process diagram showing an overview of the method of the present invention, FIG. 2 is a layout diagram of main parts of an embodiment of the apparatus used for carrying out the method of the present invention, and FIG. It is an overall layout diagram including main parts. 1... Upper tank, 2... Lower tank, 3... Cylindrical pipe, 4...
Heavy oil mixing introduction pipe, 4a, 4b... Heavy oil introduction branch pipe, 8... Heavy liquid extraction pipe, 11... Light liquid extraction pipe, 15... Light liquid circulation piping, 16... Cooling vessel, 1
7...Shelf board.

Claims (1)

[Claims] 1. An insoluble substance is produced in the heavy oil mixture by preparing a high-temperature heavy oil mixture consisting of at least two types of heavy oil, and further cooling this mixture, and the insoluble substance is When continuously producing feedstock oil for gasoline production by removing it from a heavy oil mixture, a part of the produced feedstock oil for gasoline production is extracted and circulated to the cooling process, and the flow of this circulating oil and the 1. A continuous production method for raw material oil for gasoline production, characterized in that a heavy oil mixture is cooled by contacting a stream of a high-temperature heavy oil mixture. 2. The temperature of the high-temperature heavy oil mixture is 200 to 390°C, and further cooling is performed at a temperature of 100°C or less,
A method according to claim 1. 3. The method according to claim 1, wherein the heavy oil mixture is cooled by countercurrently colliding a jet of the hot heavy oil mixture with a jet of circulating oil. 4. Before bringing the circulating oil into contact with the heavy oil mixture,
2. The method of claim 1, wherein the circulating oil is previously cooled to about 50 to about 90<0>C. 5. The method according to claim 1, wherein the high-temperature heavy oil mixture is prepared by heating at least two types of heavy oil in advance and then combining them. 6. The claimed invention, wherein the at least two types of heavy oils are selected from the group consisting of petroleum-based atmospheric or vacuum direct distillation residue oil, coal tar, naphtha cracking residue oil, thermal cracking residue oil, and hydrocracking residue oil. The method described in Scope No. 1.