KR20030053062A - Method of Refining Petroleum - Google Patents

Abstract

A petroleum refining method, comprising: a distillation separation step 1 in which raw oil is distilled and separated into effluent oil M1 and residual oil M2; Hydrorefining step 2 for hydrorefining at least a portion of the effluent oil M1, thereby obtaining hydrogenated refined oil M3; A solvent removal step 3 of deasphalting the residual oil M2 with the solvent to obtain deasphalted oil M4 and asphalt (bitumen) M5; Demetal / dehydration step 4 of at least a portion of deasphalted oil M4 to demetal / deflux to obtain HDMS refined oil M6; And a first mixing step 5 of mixing a portion of the HDMS refined oil with at least a portion of the hydrogenated refined oil M3 to obtain a petroleum product.

Description

Method of Refining Petroleum

Conventionally, as this kind of technique, the technique which can produce an individual petroleum product and its intermediate product efficiently is known as shown below, for example.

(1) The raw oil is distilled at atmospheric pressure, separated into distillate and atmospheric residue, and the resulting atmospheric residue is distilled under reduced pressure, and the vacuum residue (VR) is treated by a coker to pyrolyze gasoline and light oil. Manufacturing technology.

(2) A technique in which deasphalted oil (solvent asphalt removal oil; DAO) obtained by treating the above-mentioned atmospheric residual oil with solvent asphalt removal (SDA) as a raw material for fluid catalytic cracking (FCC), or vacuum atmospheric distillation (VDU) ), A technique in which the obtained vacuum gas (VGO) is treated as a raw material for fluid catalytic cracking (FCC).

However, the technique as described in (1) has a problem that the market of coke sediment (coke) is excessive in supply, and the construction of cokers producing coke as a by-product is restricted.

In addition, the technique shown in (2) has the following problems. Deasphalted and decompressed light oils are separated from the vast reserves of heavy oil and the atmospheric residual oil that is expected to be oversupply in the future, and introduced into fluid catalytic cracking (FCC) and hydrocracking (HCR) to provide gasoline and diesel. The production of transport fuels cannot cope with the market supply and demand balance of transport fuels and power generation fuels because the increase in electric power demand is expected to increase in the future as the demand for gasoline and diesel fuels increases worldwide.

In addition to the techniques described in (1) and (2), for example, there is a technique of performing solvent removal from ultra-heavy oil and atmospheric residual oil having a high vanadium concentration and producing a gas turbine fuel (GTF). Even if the yield (flow rate) of the deasphalted oil in the solvent removal process is increased, the contamination by the metal and residual carbon of the deasphalted oil obtained becomes high, and as a result, the load at the time of demetallizing and demetallizing such deasphalted oil becomes high. (High pressure, low LHSV) and economically disadvantageous. In addition, from this situation, lowering the yield of deasphalted oil reduces the yield of gas turbine fuel, resulting in a new problem of increased production of low value added asphalt (bitumen).

An object of the present invention is to provide a petroleum product (gas turbine fuel) having a vanadium (V) concentration of 0.5 wt ppm or less, particularly in the case of using heavy oil as a starting material and a starting material having a low sulfur concentration as a starting material. It is an object of the present invention to provide a petroleum refining method capable of efficiently producing an intermediate petroleum product as a raw material for sulfur catalytic cracking or hydrocracking having a metal concentration (V + Ni) of 30 wt ppm or less.

The present invention relates to a petroleum refining method for efficiently producing various petroleum products having high value added, and more particularly, from a heavy oil or a raw material of low sulfur concentration, having a high added value and having various specifications. The present invention relates to a method for refining petroleum products efficiently.

1 to 6 each show a processing flow for explaining the first to sixth embodiments of the petroleum refining method of the present invention.

7-12 are process flows for demonstrating the petroleum refining method of Examples 1-6, respectively.

The petroleum refining method according to the first aspect of the present invention is a petroleum refining method for refining a raw oil to produce a petroleum product including various intermediate petroleum products, wherein the raw oil is distilled to separate the effluent oil and the residual oil. At least a part of the distillation separation step and the distillation separation step are subjected to hydrorefining treatment in the presence of hydrogen and a catalyst, and dehydrogenated to obtain dehydrogenated refined oil, and solvent removal treatment of the residual oil. And a solvent removal step of obtaining deasphalted oil as the extract and the remaining asphalt (bitumen); and at least a portion of the deasphalted oil in a presence of hydrogen and a catalyst, hydrodemetallization and deflow treatment to remove demetallized and dehydrogenated HDMS refined oil. Hydrogenation demetalization and dehydration process obtained, a part of said HDMS refined oil, and at least a part of the said deflowed refined oil are mixed, And a first mixing step of obtaining one of the petroleum products.

According to this refining method, since at least a part of demineralized refined oil is mixed with a part of HDMS refined oil in the first mixing step, it is thus possible to obtain a petroleum product having a sufficiently low vanadium (V) concentration such as a gas turbine fuel. In addition, it is possible to obtain an intermediate petroleum product having a relatively low metal concentration (V + Ni) from the remainder of the HDMS refined oil and a raw material for fluid catalytic cracking or hydrocracking.

In addition, in the intermediate petroleum product as a raw material for fluid catalytic cracking or hydrocracking, since the allowable concentration for metal is higher than that of gas turbine fuel, etc., the gas turbine fuel and the raw material for fluid contacting or hydrocracking are produced together. It is possible to increase the yield of deasphalted oil by the solvent removal step, whereby it becomes possible to suppress the by-product amount of asphalt (bitumen) from atmospheric residual oil.

In the petroleum refining method according to the second aspect of the present invention, a distillation process for distilling raw oil to separate the effluent oil and the residual oil, and at least a portion of the effluent oil obtained in the distillation separation process in the presence of hydrogen and a catalyst for hydrogenation purification Hydrogen purifying step of obtaining de-refined refined oil by degassing, solvent removal treatment of the residual oil, solvent removal step of obtaining deasphalted oil as extract and remaining asphalt (bitumen), and at least a part of deasphalted oil And a hydrodemetallization and dehydration process for obtaining a dehydrogenated and dehydrogenated HDMS refined oil in the presence of a catalyst and a catalyst, and distillation under reduced pressure distillation of the HDMS refined oil under reduced pressure distillation under reduced pressure to obtain a gas oil and a vacuum residue. Process and mixing at least a portion of the vacuum gas oil and at least a portion of the de-refined refined oil, A second mixing step of obtaining one of the arms.

According to this method, since at least a portion of the reduced-pressure diesel oil and at least a portion of the de-refined refined oil are mixed in the second mixing step, it is thus possible to obtain a petroleum product having a sufficiently low vanadium (V) concentration such as, for example, a gas turbine fuel. It is possible. Moreover, it is possible to obtain an intermediate petroleum product as a raw material for fluid catalytic cracking or hydrocracking, even from the remainder of vacuum gas oil and the vacuum residual oil obtained by the pressure-reducing process, especially HDMS refined oil, with comparatively low metal concentration (V + Ni).

In addition, the HDMS refined oil was distilled under reduced pressure by a vacuum distillation process, so that the metal portion and the residual carbon portion were separated from the distillation phase boiling point with less vacuum gas oil and reduced pressure residual oil, so that the vanadium concentration of the HDMS refined oil itself and It is possible to allow the metal concentration to a relatively high concentration, whereby it is possible to increase the yield of deasphalted oil by the solvent removal step, thus making it possible to suppress the by-product amount of asphalt (bitumen) from atmospheric residual oil. do.

In the petroleum refining method according to the third aspect of the present invention, a distillation step of distilling a raw material oil into a effluent oil and a residual oil, and at least a portion of the effluent oil obtained in the distillation separation step are hydrorefining treatment in the presence of hydrogen and a catalyst. And a hydrorefining step of distilling the residual oil under reduced pressure distillation to separate the residual oil into a reduced pressure diesel oil and a reduced pressure residue, and removing the reduced pressure residue by solvent removal to remove the deasphalted oil as an extract. And a solvent removal treatment step for obtaining the remaining asphalt (bitumen), and the vacuum gas and deasphalted oil, and the mixed oil was subjected to hydrodemetallization and deflow treatment in the presence of hydrogen and a catalyst, followed by demetallization and dehydration purification. Hydrogenation demetalation and dehydration process of obtaining HDMS refined oil, a part of said HDMS refined oil, and at least a part of said deflowed refined oil Mixed, and a third mixing step of obtaining one of the oil products.

According to this method, since a part of HDMS refined oil and at least a part of de-refined refined oil are mixed in the third mixing step, the vanadium (V) concentration of the obtained mixed oil is sufficiently lowered to obtain a petroleum product as a gas turbine fuel. Do. Furthermore, from the remainder of the HDMS refined oil obtained by hydrodemetallizing and deflowing the mixed liquid of reduced pressure diesel fuel and deasphalted oil, it is also possible to obtain an intermediate petroleum product having a low metal concentration (V + Ni) as a raw material for fluid catalytic cracking or hydrocracking. It is possible.

In addition, in the case of intermediate petroleum products as raw materials for fluid catalytic cracking or hydrocracking, the allowable concentration of methane is higher than that of gas turbine fuel and the like. Therefore, solvents are produced by simultaneously producing gas turbine fuel and raw materials for fluidic contact or hydrocracking. It is possible to increase the yield of deasphalted oil by the removal step, thus making it possible to suppress the by-product amount of asphalt (bitumen) from the vacuum residue.

In addition, when the present invention is applied to heavy oil having an API degree of 20 or less, it is possible to reduce the amount of bitumen produced, and to recover various petroleum products having high added value, as compared with the conventional art which has produced a large amount of bitumen having a low commodity value. The productivity is greatly improved.

A petroleum refining method according to a fourth aspect of the present invention is a petroleum refining method for producing a petroleum product including various intermediate petroleum products by refining a raw material oil to a raw material having a low sulfur concentration. Distillation to separate the effluent oil and the residual oil into distillation, solvent removal treatment of the residual oil obtained in the distillation separation process to obtain deasphalted oil as the extract and the remaining asphalt (bitumen), and A hydrodemetallizing process for obtaining at least a portion of asphalt oil in the presence of hydrogen and a catalyst for hydrodemetallizing and deflowing to obtain demetallization and deflow-refining HDMS refined oil, a portion of the HDMS refined oil and at least a portion of the effluent oil are mixed. And a fourth mixing step of obtaining one of the petroleum products.

According to this method, since a part of HDMS refined oil and at least a part of demineralized refined oil are mixed in the fourth mixing step, it is possible to obtain a petroleum product having a low vanadium (V) concentration such as, for example, a gas turbine fuel. In addition, it is possible to obtain an intermediate petroleum product as a raw material for fluid catalytic cracking or hydrocracking having a relatively low metal concentration (V + Ni) from the remainder of the HDMS refined oil.

In addition, in the case of intermediate petroleum products as raw materials for fluid catalytic cracking or hydrocracking, the allowable concentration of methane is higher than that of gas turbine fuel and the like. Thus, solvents are produced by simultaneously producing gas turbine fuel and raw materials for fluid catalytic cracking or hydrocracking. It is possible to increase the yield of deasphalted oil by the removal step, thus making it possible to suppress the by-product amount of asphalt (bitumen) from atmospheric residual oil.

The petroleum refining method according to the fifth aspect of the present invention is a distillation separation step of distilling raw oil to separate effluent oil and residual oil, and solvent removal treatment of the residual oil obtained in the distillation separation step. Solvent removal treatment process to obtain phosphorus asphalt (bitumen), and hydrodemetalization process to obtain at least a part of the deasphalted oil in the presence of hydrogen and a catalyst by hydrodemetallizing and deflowing to obtain demetallization and deflow-refining HDMS refined oil. And a vacuum distillation separation step of distilling the HDMS refined oil under reduced pressure to separate the vacuum light oil and the vacuum residual oil, and a fifth mixing step of mixing at least a portion of the vacuum gas oil with at least a portion of the effluent oil to obtain one of the petroleum products. It includes.

According to this method, since at least a part of the vacuum gas oil and at least a part of the outflow oil are mixed in the fifth mixing step, it is possible to obtain a petroleum product having a sufficiently low vanadium (V) concentration such as, for example, a gas turbine fuel. Do. In addition, it is possible to obtain an intermediate petroleum product as a raw material for fluid catalytic cracking or hydrocracking with a relatively low metal concentration (V + Ni) also from the remainder of the vacuum gas oil and the vacuum residue obtained by vacuum distillation, in particular, the remainder of the HDMS refined oil. Do.

In addition, in particular, by vacuum distillation, the HDMS refined oil is subjected to reduced pressure distillation so that the metal portion and the residual carbon portion are separated from the boiling point of the distillate phase into a reduced pressure gas oil and a reduced pressure residual oil, so that the vanadium concentration and the methane concentration of the HDMS itself are reduced. It is possible to allow up to a relatively high concentration, thus making it possible to suppress the by-product amount of asphalt (bitumen) from atmospheric residual oil.

In the petroleum refining method according to the sixth aspect of the present invention, there is provided a distillation process for distilling crude oil to separate the effluent oil and the residual oil, and distilling the residual oil obtained in the distillation separation process under reduced pressure to separate the light oil and the reduced pressure oil. The vacuum distillation separation process, the solvent removal treatment of the said vacuum residue, the solvent removal process of obtaining the deasphalted oil as an extract and the remainder asphalt (bitumen), and the said vacuum gas oil and deasphalted oil are mixed, and this mixed oil is mixed. A hydrodemetalization / deflow process for obtaining a dehydrometallization and deflow-refined HDMS refined oil in the presence of hydrogen and a catalyst, and a portion of the HDMS refined oil and at least a portion of the effluent oil are mixed to produce a petroleum product. A sixth mixing process of obtaining one is included.

According to this method, since a part of HDMS refined oil and at least a part of effluent oil are mixed in the sixth mixing step, the vanadium (V) concentration of the obtained mixed oil is sufficiently lowered, and it is possible to obtain a petroleum product as a gas turbine fuel. Furthermore, an intermediate petroleum product as a raw material for fluid catalytic cracking or hydrocracking having a low metal concentration (V + Ni) can also be obtained from the remainder of the HDMS refined oil obtained by hydrodemetallizing and deflowing the mixed oil of reduced pressure diesel fuel and deasphalted oil. It is possible.

In addition, in the case of intermediate petroleum products as raw materials for fluid catalytic cracking or hydrocracking, the allowable concentration of methane is higher than that of gas turbine fuel and the like. Therefore, solvents are produced by simultaneously producing gas turbine fuel and raw materials for fluidic contact or hydrocracking. It is possible to increase the yield of deasphalted oil by the removal step, thus making it possible to suppress the by-product amount of asphalt (bitumen) from the vacuum residue.

In addition, when the method of the fourth to sixth embodiments is applied to low-sulfur crude oil having a sulfur concentration of 2.0 wt% or less, it is preferable to reduce the amount of bitumen produced in comparison with the prior art which has produced a large amount of bitumen having a low commodity value. It is possible to increase the recovery rate of various high value added petroleum products, and greatly improve the productivity.

EMBODIMENT OF THE INVENTION Hereinafter, the preferred embodiment of the petroleum refining method which concerns on this invention is described, referring drawings. However, the present invention is not limited to the following embodiments, and for example, those similar to the components of these embodiments may be appropriately combined.

[First Embodiment]

1 is a process flow diagram for explaining an embodiment of the petroleum refining method of the present invention, in particular, using heavy oil as raw material oil, and from them, gas turbine fuel (GTF) and fluid catalytic cracking (FCC) fuel or hydrogenation The processing flow in the case of producing the decomposition (HCR) fuel together is shown.

The raw material oil to be treated is not particularly limited, and can be applied to hydrocarbon oils from crude oil to heavy oil. However, when applied to heavy oils such as Orinoco tar, especially heavy oils having an API degree of 20 or less, An example in which the yield is remarkably improved will be described.

The API diagram is an index for classifying crude oil into physical properties, and is an expression derived by its specific gravity as shown in the following equation. S represents specific gravity at 60 degrees Fahrenheit.

API = (141.5 / S)-131.5

In the method of the present embodiment, such heavy oil is used as the raw material oil, first, the raw material oil is sent to the distillation separation step 1, and the distillation process similar to the conventional one is used to separate the effluent oil M1 having low boiling point and the residual oil M2 having a higher boiling point than this. do. As the apparatus for performing the distillation treatment, a topper, which is generally an atmospheric distillation apparatus, can be preferably used, but is not particularly limited as long as it is a distillation separation means. Moreover, it is also preferable to distill and collect collectively, without dividing an effluent oil, and it is also preferable to collect effluent oil by dividing into many at boiling point. In the case of recovery by dividing into a large number, if the obtained effluent oil satisfies the specifications of the petroleum component, the hydrogenation step 2 which is the next step can be bypassed and omitted as indicated by arrow 11.

Subsequently, at least a part of the distillate oil M1 obtained in the distillation separation process 1 is sent to a hydrorefining process (HT process) 2, and the hydrorefining process is carried out in the presence of hydrogen and a catalyst, followed by dehydration to obtain hydrogenated refined oils M3 and M3 '. will be.

As a hydrorefining process for the distillate oil M1, hydrogen gas is mixed with the distillate oil M1, introduced into a reactor filled with a CoMo catalyst or a NiMo catalyst, and hydrogenated and desulfurized the sulfur and nitrogen components contained in the distillate oil M1 under the conditions of high pressure hydrogen. After denitrification, hydrogen gas is separated in a high pressure separator to obtain hydrogenated refined oils M3 and M3 '.

Apart from the hydrorefining step 2, the residual oil M2 obtained in the distillation separation step 1 is sent to a solvent removal step (SDA step) 3, and the solvent removal treatment is performed to remove deasphalted oil (DAO) M4 and asphalt (bitumen) M5 as extracts. Get

As the solvent removal treatment, first, the residual oil M2 is subjected to countercurrent contact with the solvent in a solvent extraction column so that the deasphalted oil is separated into asphalt (bitumen) in which metal and residual carbon are concentrated. It is obtained by recovering together with the solvent from the deasphalted oil and the top of the column, and separating and removing the solvent in the recovered product in a supercritical state. Asphalt (bitumen) is recovered with the solvent from the bottom of the tower, and the solvent in the recovered product is removed by evaporation.

In general, in the solvent removal step, it is known that the extraction rate of sulfur, vanadium, nitrogen, residual carbon, and the like contained in asphalt oil, which is the extraction rate with respect to the feedstock oil, is different for each component. In the present invention, when the residual oil obtained by distilling heavy oil is used as a raw material, the vanadium concentration in the deasphalted oil with respect to the vanadium concentration in the raw material oil is vanadium extraction rate. In the case of residual oil, it is preferable to set it as 15% or less. In each case, the lower limit of the extraction rate is not specified, and an appropriate range can be selected according to the type of raw oil supplied, the vanadium concentration, and the like. In the case of using the residual oil obtained by distilling off the low sulfur raw material oil having a sulfur concentration of 2.0 wt% or less as a raw material, the vanadium concentration in the deasphalted oil is 25 wt ppm or less in the case of atmospheric distillation residual oil, and in the case of a vacuum distillation residual oil. It is preferable to set it as 70 wt ppm or less.

According to the present invention, refined oil can be efficiently obtained by maximizing the extraction rate of the solvent removal step without placing a heavy load on the hydrodemetalization and degassing step at the end of the solvent removal step.

In the case where the purification step from the solvent removal step 3 to the subsequent stage is only the hydrogenation demetalization and deflow step 4, the solvent removal step 3 has a 20% extraction rate of vanadium in the deasphalted oil M4 obtained with respect to vanadium (V) in the residual oil M2 as the feedstock. It is preferable to control the extraction rate so as to be below.

At least a portion of the deasphalted oil M4 obtained in the solvent removal step 3 is sent to a hydrodemetalization / deflow process (HDMS process) 4, hydrodemetallization and deflow treatment in the presence of hydrogen and a catalyst, and demetallization and dehydration purification. Obtain HDMS refined oil M6. This hydrogenation demetal-dehydration process is basically the same as that of the hydrorefining process (hydrogenation refining process 2) mentioned above, and description is abbreviate | omitted.

Regarding the HDMS refined oil M6 obtained by such hydrodemetalization and deflow treatment, the vanadium (V) concentration is 2 wt ppm or less, preferably 1 wt ppm or less, and the sulfur concentration is 0.5 wt% or less. It is preferable to select demetal-deflow condition so that it may become 0.3 wt% or less preferably.

Particularly, a part of the HDMS refined oil M6 obtained in the hydrodemetalization and deflow process 4 and at least a part of the hydrogenated refined oil M3 obtained in the hydrorefining process 2 are sent to the first mixing process 5 to be mixed to obtain a petroleum product.

When the petroleum product obtained in such a 1st mixing process 5 is made into gas turbine fuel (GTF), mixing conditions are set so that the vanadium (V) concentration may be 0.5 wt ppm or less. In that case, for example, if the V concentration of HDMS refined oil M6 is 1 wt ppm, the V concentration of hydrogenated refined oil M3 is 0 wt ppm, and the capacity ratio of HDMS refined oil M6 and hydrogenated refined oil M3 is 1: 1 or less. Mix (ie, less HDMS refined oil M6).

In addition, among the HDMS refined oil M6 obtained in the hydrodemetalization / deflow process 4, the remainder not provided in the first mixing process 5 is used as a raw material for fluid catalytic cracking (FCC) or a hydrocracking (HCR). It is used as an intermediate petroleum product. In particular, in the hydrogenated refined oil M3, the remainder not provided in the first mixing step 5 can be set to petroleum products M3 'such as naphtha, gasoline, kerosene and the like.

According to this petroleum refining method, since at least a part of the hydrogenated refined oil M3 is mixed with a part of the HDMS refined oil M6, it is thereby possible to obtain a petroleum product having a sufficiently low vanadium (V) concentration such as, for example, a gas turbine fuel. In addition, it is possible to obtain intermediate petroleum products as fluid catalytic cracking (FCC) or hydrocracking raw materials (HCR) having a relatively low metal concentration (V + Ni) from the remainder of the HDMS refined oil M6, and have a high added value. It is possible to produce products together efficiently.

In addition, the intermediate petroleum products as fluid catalytic cracking (FCC) or hydrocracking raw materials (HCR) have a higher allowable concentration for metals than gas turbine fuels (GTF), etc. It is possible to raise the yield of deasphalted oil M4 by the solvent removal process 3, and it is possible to suppress the by-product amount of asphalt (bitumen) M5 from residual oil M2 by this.

In addition, in the processing flow shown in FIG. 1, fluid catalytic cracking is carried out by mixing with a part of HDMS refined oil having a relatively low metal concentration and a sulfur concentration and a particularly low metal concentration and a sulfur concentration in the deasphalted oil M4 obtained in the solvent removal step 3. When the raw material properties of the solvent (FCC) and hydrocracking (HCR) are satisfied, a part of the HDMS refined oil M6 is passed through the bypass shown by reference numeral 12 in FIG. It may be mixed with and used as an intermediate petroleum product as a raw material for fluid catalytic cracking (FCC) and a hydrocracking (HCR) raw material.

Second Embodiment

FIG. 2 is a processing flow for explaining the second embodiment of the petroleum refining method of the present invention, which is similar to the first embodiment shown in FIG. To produce a fluid catalytic cracking (FCC) raw material or a hydrocracking (HCR) raw material together.

The second embodiment differs mainly from the first embodiment shown in FIG. 1 in that the obtained HDMS refined oil M6 is subjected to vacuum distillation under reduced pressure at the end of the hydrodemetallization and dehydration step 4 to separate the vacuum gas oil M7 and the vacuum residue M8. It is the point which designed the vacuum distillation separation process 6. That is, in the petroleum refining method shown in FIG. 2, the HDMS refined oil M6 obtained in a similar manner to the example shown in FIG. 1 is sent to the vacuum distillation separation step 6, and subjected to vacuum distillation.

In this vacuum distillation process, HDMS refined oil M6 is introduced into a reduced pressure distillation column to distill, and the low boiling point component and the high boiling point component in HDMS refined oil M6 are separated, and the low boiling point reduced pressure diesel oil M7 is separated from the top of the tower and further heated from the bottom of the column. The vacuum residue M8 of a point is obtained, respectively.

In order to perform such vacuum distillation, in this example, the extraction rate of vanadium in deasphalted oil M4 obtained with respect to vanadium (V) in residual oil M2 which is a feedstock is 30 with respect to the deasphalted oil M4 obtained by the said solvent removal process. It is preferable to limit it to% or less. Thereby, it becomes possible to raise the recovery rate of a petroleum product, without putting a big burden on the backside hydrodemetalization and deflow process.

In addition, regarding HDMS refined oil M6 obtained by hydrodemetalization and dehydration of such deasphalted oil M4, the demetallurgical and vanadium (V) concentration is 20 wt ppm or less, preferably 10 wt ppm or less. In addition to selecting the desulfurization conditions, the sulfur concentration is preferably 0.5 wt% or less, preferably 0.3 wt% or less.

In particular, with respect to the vacuum gas oil obtained by vacuum distillation of such HDMS refined oil M6, the vanadium concentration is preferably 1 wt ppm or less.

After such a step, at least a portion of the reduced pressure diesel oil M7 obtained in the vacuum distillation separation process 6 and at least a portion of the hydrogenated refined oil M3 obtained in the hydrorefining process 2 are sent to the second mixing process 7 and mixed to obtain one of the petroleum products.

In the case where the petroleum product obtained in the second mixing step 7 is a gas turbine fuel (GTF), the vanadium (V) concentration is 0.5 wt ppm or less, similarly to the example shown in FIG. Similarly to the example, the mixing ratio is appropriately adjusted by the V concentration of the vacuum gas oil M7. In addition, when the vanadium (V) concentration of the vacuum gas oil M7 is 0.5 wt ppm or less, the gas turbine fuel (GTF) may be used as it is without adding hydrogenated refined oil M3.

The residue of vacuum gas M7 and the vacuum residue M8 obtained by distillation under reduced pressure, in particular HDMS refined oil M6, were subjected to vacuum distillation to separate the vacuum gas M7 containing little metal and residual carbon and the vacuum residue M8 from the boiling point range of the distillation phase. Therefore, it is possible to allow the vanadium concentration, the metal concentration, and the residual carbon of HDMS refined oil M6 itself to a relatively high concentration, thereby increasing the yield of deasphalted oil M4 by the solvent removal step 3, and thus the residual oil. It is possible to suppress the by-product amount of asphalt (bitumen) M5 from M2.

In addition, regarding the deasphalted oil M4 obtained in the solvent removal step 3, when its vanadium (V) concentration and the like are sufficiently low, a part of the deasphalted oil M4 is introduced into bypass 12 without being sent to the hydrodehydration / deflow step 4. HDMS refined oil obtained in the hydrodesulfurization / dehydration step 4 may be used as a intermediate product as a raw material for fluid catalytic cracking (FCC) and hydrocracking (HCR) by mixing with the vacuum residue M8 from the vacuum distillation separation step 6. M6 may also be introduced into bypass 12 and mixed with the vacuum residue M8 from the vacuum distillation separation step 6 to be an intermediate petroleum product for fluid catalytic cracking (HCC) and hydrocracking raw material (HCR).

Third Embodiment

FIG. 3 is a processing flow for explaining the third embodiment of the present invention. In this method, similarly to the example shown in FIG. 1, gas turbine fuel (GTF) and fluid catalytic cracking (FCC) from raw oil are used. Alternatively, they produce raw materials for hydrocracking (HCR).

A part mainly different from the first embodiment shown in FIG. 1 is a reduced pressure distillation separation step 20 in which the residual oil M2 obtained after the distillation separation step 1 is subjected to reduced pressure distillation to separate the reduced pressure diesel fuel M11 and the reduced pressure residual oil M12; Solvent removal treatment of the obtained reduced pressure residual oil M12, the solvent removal treatment process 21 which isolate | separates into deasphalted oil M13 and asphalt (bitumen) M14, and the hydrogenation demetalization and dehydration treatment of the mixed oil of the deasphalted oil M13 and the vacuum gas oil M11 obtained. This is the point of designing the hydrodemetalization and deflow process 22 to obtain HDMS refined oil M15.

That is, in the petroleum refining method shown in FIG. 3, the residual oil M2 obtained by treating similarly to the example shown in FIG. 1 is sent to the reduced-pressure distillation separation process 20, and it is subjected to reduced-pressure distillation.

In such a vacuum distillation separation process, the residual oil M2 is sent to a vacuum distillation column for distillation, and separated into a low boiling point portion and a high boiling point portion in the residual oil M2, and the reduced pressure diesel oil M11 having a low boiling point component is removed from the top of the tower from the bottom of the tower. Obtain Residual Oil M12, respectively.

After the reduced pressure distillation separation process 20, the obtained reduced pressure residual oil M12 is sent to the solvent removal process process 21, and it isolate | separates into deasphalted oil M13 and asphalt oil (bitumen) M14. This solvent removal treatment process is similar to the example shown in Figs. 1 and 2, but since the metal, residual carbon, and sulfur portions are more concentrated than the residual oil M2, deasphalting obtained by the solvent removal treatment process of the vacuum residual oil is carried out. With respect to the oil M13, the desired upper limit of the extraction rate of vanadium (V) is lowered, and it is preferable to control the extraction rate to be 15%.

Subsequently, deasphalted oil M13 obtained in this way and the said vacuum gas oil M11 are mixed, and this mixed oil is subjected to hydrodemetalization and deflow process to obtain HDMS refined oil M15. Regarding the obtained HDMS refined oil M15, the vanadium (V) concentration was 2 wt ppm or less, preferably 1 wt ppm or less, and the sulfur concentration was 0.5 wt ppm, preferably 0.3 wt ppm or less. It is preferable to select metal and dehydration conditions.

Thereafter, a part of the HDMS refined oil M15 obtained in the hydrodemetalization / deflow process 22 and at least a portion of the hydrogenated refined oil M3 obtained in the hydrorefining process 2 were sent to the third mixing process 23, and the vanadium (V) concentration was 0.5. Gas turbine fuel (GTF) is obtained as one of the petroleum products that is wt ppm or less.

In the HDMS refined oil M15 obtained in the hydrodemetalization / deflow process 22, the remainder not provided in the third mixing process 23 is used as a raw material for fluid catalytic cracking (FCC) or a hydrocracking (HCR) raw material. It is possible to do with petroleum products.

When the deasphalted oil M13 and the reduced pressure diesel oil M11 each contain significantly different concentrations of the metal part, the residual carbon, and the sulfur part, and there is a large difference in the reaction conditions, particularly the hydrogen partial pressure, separate reactors are not mixed. In each of the conditions under optimum conditions, hydrodemetallization and deflow treatment were carried out, and then, at least a portion of the vacuum gas M11 mixed or hydrodemetallization and deflow treatment and at least a portion of the hydrogenated refined oil M3 were mixed, and the vanadium (V) concentration was adjusted. It is also possible to obtain a gas turbine fuel (GTF) that is 0.5 wt ppm or less.

According to this petroleum refining method, since a part of HDMS refined oil M15 and at least a portion of hydrogenated refined oil M3 were mixed in the third mixing step 23, the vanadium (V) concentration of the obtained mixed oil was sufficiently low, and the gas as one of the petroleum products was It is possible to obtain a turbine fuel. In addition, from the remainder of the HDMS refined oil M15 obtained by hydrodemetallizing and deflowing the mixed oil of the reduced-pressure diesel fuel M11 and the deasphalted oil M13, it is used as a raw material for fluid catalytic cracking or hydrocracking having a low metal concentration (V + Ni). It is possible to obtain intermediate petroleum products, and to produce various petroleum products with high added value efficiently.

Intermediate petroleum products as fluid catalytic cracking (FCC) or hydrocracking (HCR) raw materials have a higher allowable concentration for metals than gas turbine fuels and the like, so that they are in fluid contact with gas turbine fuel (GTF) or hydrocracking. By producing the raw material together, it is possible to increase the yield of deasphalted oil M13 in the solvent removal treatment step 21, whereby it is possible to suppress the by-product amount of asphalt (bitumen) M14 from the vacuum residue M12.

Next, the fourth to sixth embodiments suitable for the case where low sulfur crude oil is used as the raw material oil will be described. The low sulfur crude oil in the present specification includes arabian light, iranian light, iranian heavy, marban, and crude oil whose sulfur concentration is equal to or lower than these, specifically, the sulfur concentration is 2.0 wt%. Refers to crude oil.

In the following example, since the low sulfur crude oil is used, the hydrogenation refinement | purification process (HT process) 2 is abbreviate | omitted compared with the 1st Example which made heavy oil object. In other respects, the processing similar to that of the first embodiment is basically performed. Hereinafter, the same steps as in the first embodiment will be described with A attached to the end of the code in the first embodiment.

[Example 4]

4 is a flowchart showing a fourth embodiment of the present invention. In this fourth embodiment, the low-sulfur crude oil is used as the raw material oil, and the raw material oil is first sent to the distillation separation step 1A, and the distillation treatment similar to the conventional one is performed, and the effluent oil M1A made up of the low boiling point and the residual oil M2A having a higher boiling point than this. Separate. An apparatus similar to the first embodiment may be used.

The outflow oil M1A obtained in the distillation separation process 1A is separated into the outflow oil M3A and M3A 'by a flasher 30.

The residue oil M2A obtained in the distillation separation step 1A is sent to the solvent removal treatment step (SDA step) 3A, and the solvent removal treatment is performed to obtain deasphalted oil (DAO) M4A and asphalt (bitumen) M5A as extracts.

As the solvent removal treatment, first, the residual oil M2A is separated into a deasphalted oil and asphalt (bitumen) in which metal and residual carbon are concentrated by making a countercurrent contact with the solvent in a solvent extraction column. Deasphalted oil is recovered from the top of the column with the solvent and is obtained by separating and removing the solvent in the recovered product in a supercritical state. Asphalt (bitumen) is recovered together with the solvent from the bottom of the column, and the solvent in the recovered product is removed by evaporation.

In the case where the refining process of the solvent removal treatment step 3A to the subsequent stage is only the hydrogenation demetallization and dehydration step 4A, it is preferable to control the extraction rate of the solvent removal treatment so that the vanadium (V) concentration of the deasphalted oil M4A is 25 wt ppm or less. .

At least a portion of the deasphalted oil M4A obtained in the solvent removal treatment step 3A is sent to a hydrodemetalization and degassing step (HDMS step) 4A, hydrodemetallization and deflow treatment in the presence of hydrogen and a catalyst, and demetallizing and depurification. One HDMS refined oil M6A is obtained. Since this hydrodehydration and deflow process is basically similar to the said hydrorefining process (hydrogenation refining process 2) for heavy oil, description is abbreviate | omitted.

Hydrogenation demetal-dehydration treatment conditions, based on the obtained HDMS refined oil M6, the vanadium (V) concentration to 2 wt ppm or less, preferably 1 wt ppm or less, and 0.5 wt% of the sulfur concentration of HDMS refined oil M6A. Hereinafter, it is preferable to select demetal-dehydration conditions so that it may become 0.3 wt% or less preferably.

A part of the HDMS refined oil M6A obtained in the hydrodemetalization and deflow process 4A and at least a part of the effluent oil M3A are sent to the fourth mixing process 5A and mixed to obtain a petroleum product.

In the case where the petroleum product obtained in the fourth mixing step 5A is used as the gas turbine fuel (GTF), the mixing conditions are set so that the vanadium (V) concentration is 0.5 wt ppm or less. For example, when the V concentration of HDMS refined oil M6A is 1 wt ppm and the V concentration of effluent oil M3A is 0 wt ppm, the capacity ratio of HDMS refined oil M6A to effluent oil M3A is 1: 1 or less (that is, Set a low HDMS refined oil M6A) and mix.

Among the residues of HDMS refined oil M6A obtained in the hydrodemetalization and deflow process 4A, which are not provided in the fourth mixing process 5A, the intermediates, which are raw materials for fluid catalytic cracking (FCC) or raw materials for hydrocracking (HCR), are used. It is made with petroleum products. Particularly, among the hydrogenated refined oil M3A, the remainder not provided in the first mixing step 5A can be set to petroleum products M3A 'such as naphtha, gasoline and kerosene.

According to this petroleum refining method, since at least a part of the hydrogenated refined oil M3A is mixed with a part of the HDMS refined oil M6A, it is possible to obtain a petroleum product having a sufficiently low vanadium (V) concentration, such as, for example, a gas turbine fuel, In addition, it is possible to obtain intermediate petroleum products as fluid catalytic cracking (FCC) or hydrocracking raw material (HCR) having a relatively low metal concentration (V + Ni) from the remainder of HDMS refined oil M6A, It is possible to produce petroleum products together efficiently.

In addition, the intermediate petroleum products as fluid catalytic cracking (FCC) or hydrocracking raw materials (HCR) have a higher allowable concentration for metals than gas turbine fuels (GTF), etc. It is not accompanied, and it is possible to raise the yield of deasphalted oil M4A by the solvent removal process 3A, and by this, it is possible to suppress the by-product amount of asphalt (bitumen) M5A from the residual oil M2A.

Further, in the processing flow shown in Fig. 4, fluid catalytic cracking is mixed with a part of HDMS refined oil having a relatively low metal concentration and a sulfur concentration, and a metal concentration and a sulfur concentration of the deasphalted oil M4A obtained in the solvent removal step 3A. When the raw material properties of the solvent (FCC) and the hydrocracking (HCR) are satisfied, a part of the HDMS refined oil M6A is passed through the bypass shown by reference numeral 12A in FIG. It may be mixed with and used as an intermediate petroleum product as a raw material for fluid catalytic cracking (FCC) and a hydrocracking (HCR) raw material.

[Example 5]

FIG. 5 is a processing flow illustrating a fifth embodiment of the present invention, and similarly to the example shown in FIG. 4, gas turbine fuel (GTF), fluid catalytic cracking (FCC) or hydrocracking ( HCR) shows the processing flow in the case of producing the raw materials together.

A part mainly different from the embodiment shown in Fig. 4 is a vacuum distillation which separates the obtained HDMS refined oil M6A under reduced pressure distillation by distillation under reduced pressure through diesel gas M7A and vacuum residual oil M8A at the end of the hydrodemetallization and degassing step 4A. This is the design of step 6A.

That is, in the petroleum refining method shown in FIG. 5, the HDMS refined oil M6A obtained in a similar manner to the example shown in FIG. 4 is sent to a reduced pressure distillation separation process 6A and subjected to reduced pressure distillation.

In such a vacuum distillation separation process, the HDMS refined oil M6A is sent to a reduced pressure distillation column to distill, and separated into a low boiling point portion and a high boiling point portion in the HDMS refined oil M6A, and a low-boiling reduced pressure diesel oil M7A from the top of the tower is further heated from the bottom of the tower. Each of the vacuum residue M8A was obtained.

Since the vacuum distillation process was performed, in the present example, the extraction rate is controlled so that the upper limit of the vanadium (V) concentration is preferably 50 ppm with respect to the deasphalted oil M4A obtained by the solvent removal treatment. It is preferable. That is, the extraction rate can be increased, and the recovery rate of petroleum products can be increased.

In addition, regarding HDMS refined oil M6A obtained by hydrodemetalization and dehydration of such deasphalted oil M4A, the demetallurgical and vanadium (V) concentration is 20 wt ppm or less, preferably 10 wt ppm or less. At the same time that the desulfurization conditions are selected, the sulfur concentration is preferably 0.5 wt% or less, preferably 0.3 wt% or less.

In particular, regarding the vacuum gas oil obtained by vacuum distillation of such HDMS refined oil M6A, the vanadium (V) concentration is preferably 1 wt ppm or less.

After this step, at least a portion of the reduced pressure diesel oil M7A obtained in the vacuum distillation separation step 6A and the outflow oil M3A are sent to the fifth mixing step 7A to be mixed to obtain one of the petroleum products.

In the case where the petroleum product obtained in the fifth mixing step 7A is used as a gas turbine fuel (GTF), the vanadium (V) concentration is made 0.5 wt ppm or less, similarly to the example shown in FIG. In that case, the mixing ratio is appropriately adjusted by the V concentration of the reduced pressure diesel gas M7A similarly to the previous example. In addition, when the vanadium (V) concentration of the vacuum gas oil M7A is 0.5 wt ppm or less, the gas turbine fuel (GTF) may be used by itself without adding the outflow oil M3A.

In addition, about the remainder which was not provided in the vacuum distillation process 6A of the vacuum residue M8A obtained by vacuum distillation and the remainder of the vacuum gas oil M7A, especially HDMS refined oil M6A, these are used for the fluid catalytic decomposition by mixing these individually or suitably. (FCC) or hydrocracking (HCR) raw materials are used to obtain intermediate petroleum products.

According to this petroleum refining method, by the vacuum distillation separation step 6A, the HDMS refined oil M6A was subjected to vacuum distillation to separate the vacuum gas oil M7A and the vacuum residue M8A containing little metal and residual carbon from the boiling point of the distillation phase. It is possible to allow the vanadium concentration, the metal concentration and the residual carbon of HDMS refined oil M6A itself to a relatively high concentration, thereby increasing the yield of deasphalted oil M4A by the solvent removal step 3A. It is possible to suppress the by-product amount of asphalt (bitumen) M5A.

Also, regarding the deasphalted oil M4A obtained in the solvent removal step 3A, when its vanadium (V) concentration and the like are sufficiently low, a part of the deasphalted oil M4A is sent to bypass 12A without being sent to the hydrodehydration / deflow step 4A. HDMS refined oil obtained by mixing with reduced-pressure residual oil M8A from vacuum distillation separation process 6A as intermediate petroleum product as a raw material for fluid catalytic cracking (FCC) and hydrocracking (HCR), and also obtained by hydrodemetalization / dehydration process 4A. M6A may also be introduced into bypass 12A and mixed with the vacuum residue M8A from vacuum distillation separation step 6A to form intermediate petroleum products as raw materials for fluid catalytic cracking (FCC) and hydrocracking (HCR).

[Example 6]

FIG. 6 is a view for explaining a sixth embodiment according to the petroleum refining method of the present invention, and similarly to the example shown in FIG. 4, gas turbine fuel (GTF) and fluid catalytic cracking (FCC) from raw oil Or the process flow at the time of producing the hydrocracking (HCR) raw material together is shown.

This embodiment is mainly different from the embodiment shown in Fig. 4, after the distillation separation step 1A, the obtained residual oil M2A is distilled under reduced pressure to obtain a reduced pressure distillation separation step 20A obtained by distillation under reduced pressure diesel oil M11A and reduced pressure residual oil M12 A. The solvent removal treatment process 21A which remove | eliminates the vacuum residual oil M12A by the solvent removal process, and isolate | separates into deasphalted oil M13A and asphalt (bitumen) M14A, and hydrogenation demetallizing and dehydrating the mixed oil of obtained deasphalted oil M13A and reduced pressure diesel oil M11A It is the point which designed the hydrogenation demetal-dehydration process 22A which obtains refined oil M15A.

That is, in the petroleum refining method shown in FIG. 6, the residual oil M2A obtained in a similar manner to the example shown in FIG. 4 is sent to a reduced pressure distillation separation process 20A for distillation under reduced pressure.

In such a vacuum distillation separation process, the residual oil M2A is sent to a vacuum distillation column to distill, and separated into the low boiling point portion and the high boiling point portion in the residual oil M2A, and the reduced pressure diesel oil M11A of the low boiling point component is further removed from the top of the tower. The vacuum residue M12A is obtained, respectively.

After such a reduced pressure distillation separation step 20A, the obtained reduced pressure residue M12A is sent to a solvent removal treatment step 21A, and separated into deasphalted oil M13A and asphalt oil (bitumen) M14A. This solvent removal treatment is similar to the examples shown in Figs. 4 and 5, but since the metal, residual carbon, and sulfur portions are more concentrated than the residual oil M2A, deasphalted oil M13A obtained by the solvent removal treatment of the vacuum residue. With respect to, the desired upper limit of the vanadium (V) concentration becomes high, and the extraction rate is controlled to be 70 wt ppm, for example.

Subsequently, deasphalted oil M13A obtained in this way and the said vacuum gas oil M11A are mixed, and this mixed oil is subjected to hydrodemetalization and deflow process to obtain HDMS refined oil M15A. Regarding the obtained HDMS refined oil M15A, the vanadium (V) concentration was 2 wt ppm or less, preferably 1 wt ppm or less, and the sulfur concentration was 0.5 wt ppm, preferably 0.3 wt ppm or less. It is preferable to select metal and dehydration conditions.

Subsequently, a part of the HDMS refined oil M15A obtained in the hydrodesulfurization and deflow process 22A and the effluent oil M3A were sent to the sixth mixing process 23A for mixing, and the gas as one of the petroleum products having a vanadium (V) concentration of 0.5 wt ppm or less. Obtain turbine fuel (GTF).

In addition, among the HDMS refined oil M15A obtained in the hydrodemetalization / deflow process 22A, the remainder not provided in the sixth mixing process 23A is regarded as a raw material for fluid catalytic cracking (FCC) or a hydrocracking (HCR) raw material. It is possible to make it into an intermediate petroleum product.

When the deasphalted oil M13A and the reduced pressure residual oil M11A each have significantly different concentrations of the metal part, the residual carbon, and the sulfur part, and there is a large difference in the reaction conditions, especially the hydrogen partial pressure, separate reactors are not mixed. In each of the conditions under optimum conditions, hydrodemetallization and deflow treatment were carried out, and then at least a portion of the reduced-pressure diesel fuel M11A mixed with the hydrodemetallization and dehydrogenation and at least a portion of the hydrogenated refined oil M3A were mixed, and the vanadium (V) concentration was adjusted. It is also possible to obtain a gas turbine fuel (GTF) that is 0.5 wt ppm or less.

According to this petroleum refining method, since a part of HDMS refined oil M15A and at least a part of effluent oil M3A were mixed in the sixth mixing step 23A, the vanadium (V) concentration of the obtained mixed oil was sufficiently low, thereby causing one of the petroleum products. As a result, it is possible to obtain a gas turbine fuel. In addition, from the remainder of the HDMS refined oil M15A obtained by hydrodemetalization and dehydration of the mixed oil of vacuum gas oil M7A and deasphalted oil M13A, the metal as a raw material for fluid catalytic cracking or hydrocracking having a low metal concentration (V + Ni) is also present. It is possible to obtain intermediate petroleum products, and to produce various petroleum products with high added value efficiently.

In addition, intermediate petroleum products as raw materials for fluid catalytic cracking (FCC) or hydrocracking (HCR) have a higher allowable concentration for metals than gas turbine fuels, etc. By producing the raw material for hydrocracking together, it is possible to increase the yield of deasphalted oil M13A according to the solvent removal treatment step 21A, thereby suppressing the by-product amount of asphalt (bitumen) M14A from the vacuum residue M12A. Do.

Experimental Example

Hereinafter, the present invention will be described in more detail with reference to experimental examples.

Experimental Example 1

Based on the petroleum refining method shown in FIG. 1, gas turbine fuels as various petroleum products and intermediate petroleum products as raw materials for fluid catalytic cracking or hydrocracking were produced together as shown in FIG.

Super heavy oil (orinoco oil) having an API degree of 8.5, a sulfur concentration of 3.67 wt%, and a vanadium concentration of 393 wt ppm was used as a raw material, and first, this was subjected to atmospheric distillation (distillation separation process 1) using a topper, Residual oil M2 was obtained. The yield of the obtained effluent oil M1 was 15.9 wt%, and the sulfur concentration was 2.41 wt%. In addition, the yield of the crude oil M2 was 83.5 wt%, the sulfur concentration was 4.07 wt%, and the vanadium concentration was 472 wt ppm.

Next, the obtained oil distillation M1 was subjected to hydrorefining treatment (hydrogenation refining step 2) in the presence of hydrogen and a catalyst, and dehydrogenated to obtain hydrogenated refined oils M3 and M3 '. M3 'was used as one of the petroleum products as naphtha. The yield of the obtained hydrogenated refined oil M3 was 13.0 wt%, and the sulfur concentration was 0.02 wt%. In addition, the yield of the raw material oil of M3 'naphtha was 2 wt%.

In addition to the hydrorefining treatment, the remaining oil M2 was subjected to solvent removal treatment (solvent removal step 3) using isobutane as a catalyst, and the deasphalted oil M4 was obtained at an extraction rate of 65%. (Bitumen) M5 was obtained. In addition, the ratio (solvent / M2) of the solvent and residual oil M2 in the solvent removal process was set to 8. The yield of the obtained deasphalted oil M4 was 54.3 wt%, the sulfur concentration was 3.60 wt%, and the vanadium concentration was 66 wt ppm (extraction rate 14%). In addition, the yield of the raw material oil of asphalt (bitumen) M5 was 29.2 wt%.

Subsequently, the obtained deasphalted oil M4 was introduced into a reactor filled with a hydrodemetalization catalyst and a hydrodehydration catalyst at a vol ratio of 3: 7, and subjected to hydrodemetalization and deflow treatment in the presence of hydrogen and the catalyst (hydrogenation demetalization and dehydration). Step 4), HDMS refined oil M6 is obtained. Further, the treatment was conducted in the conditions of hydrogen partial pressure to 100 atm, (H ₂ / oil) ratio of 800 Nl / l, a LHSV 0.7 / hr, the reaction temperature was 370 ℃. The yield of the obtained HDMS refined oil M6 was 51 wt%, the sulfur concentration was 0.4 wt%, and the vanadium concentration was 0.7 wt ppm.

Thereafter, 15 wt% (as a yield for the crude oil) in the obtained HDMS refined oil M6 was mixed with the hydrogenated refined oil M3 (first mixing step 5), the yield for the crude oil was 28 wt%, the sulfur concentration was 0.22 wt%, A gas turbine fuel (GTF) with a vanadium concentration of 0.38 wt ppm was obtained. The remainder of the HDMS refined oil M6, i.e., 36 wt% (as a yield to the crude oil), was used as raw material for fluid catalytic cracking (FCC) or hydrocracking (HCR) as it is.

Experimental Example 2

Based on the petroleum refining method shown in FIG. 2, gas turbine fuels as various petroleum products and intermediate petroleum products as raw materials for fluid catalytic cracking or hydrocracking were produced together as shown in FIG.

Super heavy oil (orinoco oil) having an API degree of 8.5, a sulfur concentration of 3.67 wt%, and a vanadium concentration of 393 wt ppm was used as a raw material, and first, this was subjected to atmospheric distillation (distillation separation process 1) using a topper, Residual oil M2 was obtained. The yield of the obtained effluent oil M1 was 15.9 wt%, and the sulfur concentration was 2.41 wt%. In addition, the yield of the crude oil M2 was 83.5 wt%, the sulfur concentration was 4.07 wt%, and the vanadium concentration was 472 wt ppm.

Next, the obtained oil distillation M1 was subjected to hydrorefining treatment (hydrogenation refining step 2) in the presence of hydrogen and a catalyst, and dehydrogenated to obtain hydrogenated refined oils M3 and M3 '. M3 'was used as one of the petroleum products as naphtha. The yield of the obtained hydrogenated refined oil M3 was 13.0 wt%, and the sulfur concentration was 0.02 wt%. In addition, the yield of the raw material oil of M3 'naphtha was 2 wt%.

In addition to the hydrorefining treatment, the remaining oil M2 was subjected to solvent removal treatment (solvent removal step 3) using pentane as a catalyst, and deasphalted oil M4 was obtained at an extraction rate of 76.6%. Bitumen) M5. In addition, the ratio (solvent / M2) of the solvent and residual oil M2 in the solvent removal process was set to 8. The yield of the obtained deasphalted oil M4 was 64 wt%, the sulfur concentration was 3.9 wt%, and the vanadium concentration was 130 wt ppm (extraction rate 27.5%). In addition, the yield of the raw material oil of asphalt (bitumen) M5 was 19.5 wt%.

Subsequently, the obtained deasphalted oil M4 was introduced into a reactor filled with a hydrogenation demetal catalyst and a hydrodehydration catalyst at a vol ratio of 5: 5, and subjected to hydrodemetalization and deflow treatment in the presence of hydrogen and the catalyst (hydrogenation demetalization and dehydration). Step 4), HDMS refined oil M6 is obtained. Further, the treatment was conducted in the conditions of hydrogen partial pressure to 100 atm, (H ₂ / oil) ratio of 800 Nl / l, a LHSV 0.5 / hr, the reaction temperature was 370 ℃. The yield of the obtained HDMS refined oil M6 was 59 wt%, the sulfur concentration was 0.45 wt%, and the vanadium concentration was 8 wt ppm.

Next, the obtained HDMS refined oil M6 was subjected to vacuum distillation (pressure distillation separation step 6) to obtain vacuum gas oil (VGO) M7 and vacuum residual M8, respectively. The yield of the obtained reduced pressure diesel oil M7 was 25 wt%, the sulfur concentration was 0.24 wt%, and the vanadium concentration was 0.3 wt ppm.

Thereafter, all of the obtained reduced pressure diesel oil M7 was mixed with the hydrogenated refined oil M3 (second mixing step 7), and the gas turbine had a yield of 38 wt% for the crude oil, a sulfur concentration of 0.16 wt%, and a vanadium concentration of 0.19 wt ppm. Fuel (GTF) was obtained. In addition, the vacuum residue M8 obtained by the vacuum distillation process was used as a raw material for fluid catalytic cracking (FCC) or a hydrocracking (HCR) raw material as it is. Furthermore, a part of deasphalted oil M4 and a part of HDMS refined oil M6 may be mixed with a reduced pressure residual oil M8 to obtain a fluid catalytic cracking (FCC) raw material or a hydrocracking (HCR) raw material. The thus obtained fluid catalytic cracking (FCC) raw material or hydrocracking (HCR) raw material had a yield of 34 wt%, a sulfur concentration of 0.60 wt%, and a vanadium concentration of 13.7 wt ppm with respect to the raw material oil.

Experimental Example 3

Based on the petroleum refining method shown in FIG. 3, gas turbine fuels as various petroleum products and intermediate petroleum products as raw materials for fluid catalytic cracking or hydrocracking were produced together as shown in FIG.

An ultra heavy oil (orinoco oil) having an API degree of 28, a sulfur concentration of 2.9 wt%, and a vanadium concentration of 69 wt ppm was used as a raw material. First, this was subjected to atmospheric distillation (distillation separation process 1) using a topper, and with effluent oil M1. Residual oil M2 was obtained. The yield of crude oil M1 thus obtained was 41 wt% and the sulfur concentration was 0.79 wt%. In addition, the yield of the crude oil M2 was 58.5 wt%, the sulfur concentration was 4.72 wt%, and the vanadium concentration was 117 wt ppm.

Next, the obtained residual oil M2 was subjected to vacuum distillation (pressure distillation separation step 20) to obtain vacuum gas oil M11 and vacuum oil residue M12, respectively. The yield of the obtained vacuum gas M11 was 28.2 wt%, the sulfur concentration was 3.37 wt%, and the vanadium concentration was 1.5 wt ppm. In addition, the yield of the obtained vacuum residue M12 was 30.6 wt%, the vanadium concentration was 223 wt ppm, the (V + Ni) concentration was 294 wt ppm, the residual carbon was 24.4 wt%, and the sulfur concentration was 6.04 wt%.

Further, each of the LPG, naphtha, kerosene, and light oil portions of the obtained oil distillate M1 was subjected to hydrorefining treatment (hydrogenation refining step 2) separately, to thereby obtain dehydrated refined oil (light portion) M3 and M3 '. The yield of the obtained hydrogenated refined oil M3 was 20.3 wt% and the sulfur concentration was 0.05 wt%. In addition, the yields of the gasoline and kerosene from the hydrogenated refined oil M3 'were 6.0 wt% and 13.7 wt%, respectively.

In addition to the hydrorefining treatment, a solvent removal treatment (solvent removal step 21) was carried out in a solvent extraction column using isobutane as a catalyst to remove deasphalted oil M13 at a 60% extraction rate. Asphalt (bitumen) M14 was obtained. In addition, the ratio (solvent / M12) of the solvent in the solvent removal process and the vacuum residue M12 was set to 8. The yield of the obtained deasphalted oil M13 was 18.4 wt%, the sulfur concentration was 4.62 wt%, and the vanadium concentration was 22 wt ppm (extraction rate 19%). In addition, the yield of the raw material oil of asphalt (bitumen) M14 was 12.2 wt%.

Subsequently, a mixed oil of the deasphalted oil M13 and the reduced pressure diesel oil M11 thus obtained was introduced into a reactor filled with a hydrodemetalization catalyst and a hydrodehydration catalyst at a vol ratio of 1: 9, and hydrogenated demetallization and dehydration in the presence of hydrogen and the catalyst. Treatment (hydrogenation demetal and dehydration step 4) afforded HDMS refined oil M15. In addition, the process is hydrogen partial pressure in the line were in a condition of 90 atm, (H ₂ / oil) of a 800 Nl / l, LHSV ratio 0.7 / hr, the reaction temperature was 370 ℃. The yield of the obtained HDMS refined oil M15 was 44 wt%, the sulfur concentration was 0.6 wt%, and the vanadium concentration was 1.0 wt ppm.

Next, in the obtained HDMS refined oil M15, 15 wt% (relative to the crude oil) was mixed with the hydrogenated refined oil M3, and a gas turbine having a yield of 45 wt% for the crude oil, a sulfur concentration of 0.28 wt%, and a vanadium concentration of 0.42 wt ppm. Got fuel. The remaining portion of the HDMS refined oil, that is, 29 wt%, was used as a raw material for fluid catalytic cracking (FCC) or hydrocracking (HCR) as it is.

Next, an experimental example using low sulfur crude oil will be described.

Experimental Example 4

Based on the petroleum refining method shown in FIG. 4, gas turbine fuels as various petroleum products and intermediate petroleum products as raw materials for fluid catalytic cracking or hydrocracking were produced together as shown in FIG.

Low-sulfur crude oil (Arabian Lite) having a sulfur concentration of 1.79 wt% and a vanadium concentration of 13.5 wt ppm was used as a raw material. At first, atmospheric distillation (distillation separation process 1A) was carried out using a topper to obtain effluent oil M1A and residual oil M2A. The yield of crude oil M1A obtained was 53.5 wt% and the sulfur concentration was 0.63 wt%. In addition, the yield of crude oil M2A was 45.4 wt%, the sulfur concentration was 3.20 wt%, and the vanadium concentration was 30.0 wt ppm.

Next, the obtained oil spill M1A was isolate | separated by the flasher 30, and oil spill M3A and M3A 'were obtained. M3A 'was used as one of the petroleum products as naphtha. The yield of crude oil M3A obtained was 50.9 wt% and sulfur concentration was 0.66 wt%. In addition, the yield of the naphtha M3A 'with respect to the raw material oil was 2.6 wt%.

The remaining oil M2A was subjected to solvent removal treatment (solvent removal step 3A) using isobutane as a catalyst, and deasphalted oil M4A was obtained at an extraction rate of 65%, and the remaining asphalt (bitumen) M5A was obtained. In addition, the ratio (solvent / M2A) of the solvent and residual oil M2A in the solvent removal process was set to 8. The yield of the obtained deasphalted oil M4A was 38.6 wt%, the sulfur concentration was 2.80 wt%, and the vanadium concentration was 5.9 wt ppm (extraction rate 19%). In addition, the yield of the raw material oil of asphalt (bitumen) M5A was 6.8 wt%.

Subsequently, the obtained deasphalted oil M4A was introduced into a reactor filled with a hydrogenation demetal catalyst and a hydrodehydration catalyst at a vol ratio of 1: 9, and subjected to hydrodemetalization and deflow treatment in the presence of hydrogen and the catalyst (hydrogenation demetalization and dehydration). Step 4A), HDMS refined oil M6A was obtained. Further, the treatment was conducted in the conditions of hydrogen partial pressure to 100 atm, (H ₂ / oil) ratio of 800 Nl / l, a LHSV 0.5 / hr, the reaction temperature was 370 ℃. The yield of the obtained HDMS refined oil M6A was 36.3 wt%, the sulfur concentration was 0.10 wt%, and the vanadium concentration was 0.9 wt ppm.

Next, in the obtained HDMS refined oil M6A, 22.7 wt% (as a yield for the crude oil) was mixed with the effluent oil M3A (fourth mixing step 5A), the yield for the crude oil was 73.6 wt%, the sulfur concentration was 0.49 wt%, vanadium A gas turbine fuel (GTF) with a concentration of 0.28 wt ppm was obtained. In addition, the remainder of HDMS refined oil M6A, i.e., 13.6 wt% (as a yield for crude oil), was used as it was as a raw material for fluid catalytic cracking (FCC) or for hydrocracking (HCR).

Experimental Example 5

Based on the petroleum refining method shown in FIG. 5, gas turbine fuels as various petroleum products and intermediate petroleum products as raw materials for fluid catalytic cracking or hydrocracking were produced together as shown in FIG.

Crude oil (Arabian Lite) having a sulfur concentration of 1.79 wt% and a vanadium concentration of 13.5 wt ppm, which is the same crude sulfur as in Experimental Example 4, was used as a raw material. M1A and residual M2A were obtained. The yield of crude oil M1A obtained was 53.5 wt% and the sulfur concentration was 0.63 wt%. In addition, the yield of the crude oil M2A was 45.4 wt%, the sulfur concentration was 3.20 wt%, and the vanadium concentration was 30.0 wt ppm.

Next, the obtained oil spill M1A was isolate | separated by the flasher 30, and oil spill M3A and M3A 'were obtained. M3A 'was used as one of the petroleum products as naphtha. The yield of crude oil M3A obtained was 50.9 wt% and sulfur concentration was 0.66 wt%. In addition, the yield of the naphtha M3A 'with respect to the raw material oil was 2.6 wt%.

In addition to the hydrorefining treatment, the remaining oil M2A was subjected to solvent removal treatment (solvent removal step 3A) using pentane as a catalyst, and deasphalted oil M4A was obtained at an extraction rate of 65%. Bitumen) M5A. In addition, the ratio (solvent / M2A) of the solvent and residual oil M2A in the solvent removal process was set to 8. The yield of the obtained deasphalted oil M4A was 38.6 wt%, the sulfur concentration was 2.80 wt%, and the vanadium concentration was 5.9 wt ppm (extraction rate 19%). In addition, the yield of the raw material oil of asphalt (bitumen) M5A was 6.8 wt%.

Subsequently, the obtained deasphalted oil M4A was introduced into a reactor filled with a hydrogenation demetal catalyst and a hydrodehydration catalyst at a vol ratio of 1: 9, and subjected to hydrodemetalization and deflow treatment in the presence of hydrogen and the catalyst (hydrogenation demetalization and dehydration). Step 4A), HDMS refined oil M6A was obtained. Further, the treatment was conducted in the conditions of hydrogen partial pressure to 100 atm, (H ₂ / oil) ratio of 800 Nl / l, a LHSV 0.7 / hr, the reaction temperature was 360 ℃. The yield of the obtained HDMS refined oil M6A was 36.3 wt%, the sulfur concentration was 0.30 wt%, and the vanadium concentration was 1.5 wt ppm.

Next, the obtained HDMS refined oil M6A was subjected to vacuum distillation (pressure distillation separation step 6A) to obtain vacuum gas oil (VGO) M7A and vacuum residue M8A, respectively. The yield of the obtained reduced pressure diesel oil M7A was 23.0 wt%, the sulfur concentration was 0.10 wt%, and the vanadium concentration was 0.2 wt ppm.

Thereafter, all of the obtained reduced pressure diesel oil M7A was mixed with the outflow oil M3A (fifth mixing step 7A), and the gas turbine fuel having a yield of raw material oil of 73.9 wt%, a sulfur concentration of 0.49 wt%, and a vanadium concentration of 0.06 wt ppm. (GTF) was obtained. In addition, the vacuum residue M8A obtained by the vacuum distillation process was used as a raw material for fluid catalytic cracking (FCC) or a hydrocracking (HCR) raw material as it was. In addition, a part of deasphalted oil M4A and a part of HDMS refined oil M6A may be mixed with a reduced pressure residual oil M8A to obtain a fluid catalytic cracking (FCC) raw material or a hydrocracking (HCR) raw material. The thus obtained fluid catalytic cracking (FCC) raw material or hydrocracking (HCR) raw material had a yield of raw material oil of 13.3 wt%, sulfur concentration of 0.65 wt%, and vanadium concentration of 3.7 wt ppm.

Experimental Example 6

Based on the petroleum refining method shown in FIG. 6, gas turbine fuels as various petroleum products and intermediate petroleum products as raw materials for fluid catalytic cracking or hydrocracking were produced together as shown in FIG.

Crude oil (Arabian Lite) having a sulfur concentration of 1.79 wt% and a vanadium concentration of 13.5 wt ppm, which is the same crude sulfur as in Experimental Example 4, was used as a raw material. M1A and residual M2A were obtained. The yield of crude oil M1A obtained was 53.5 wt% and the sulfur concentration was 0.63 wt%. In addition, the yield of the crude oil M2A was 45.4 wt%, the sulfur concentration was 3.20 wt%, and the vanadium concentration was 30.0 wt ppm.

Next, the obtained residual oil M2A was subjected to vacuum distillation (reduced pressure distillation separation step 20A) to obtain vacuum gas oil M11A and vacuum residual oil M12A, respectively. The yield of the obtained reduced pressure diesel oil M11A was 30.4 wt%, the sulfur concentration was 2.70 wt%, and the vanadium concentration was 0.1 wt ppm. In addition, the yield of the obtained vacuum residue M12A was 15.0 wt%, the vanadium concentration was 91.0 wt ppm, and the sulfur concentration was 4.10 wt%.

The obtained oil spill M1A was isolate | separated with the flasher 30, and oil spill M3A and M3A 'were obtained. M3A 'was used as one of the petroleum products as naphtha. The yield of crude oil M3A obtained was 50.9 wt% and sulfur concentration was 0.66 wt%. In addition, the yield of the naphtha M3A 'with respect to the raw material oil was 2.6 wt%.

In addition to the hydrorefining process, a solvent removal treatment (solvent removal step 21A) was carried out in a solvent extraction column using isobutane as a catalyst, and deasphalted oil M13A was obtained at an extraction rate of 60%. Asphalt (bitumen) M14A was obtained. In addition, the ratio (solvent / M12A) of the solvent in the solvent removal process and the vacuum residue M12A was set to 8. The yield of the obtained deasphalted oil M13A was 10.5 wt%, the sulfur concentration was 3.30 wt%, and the vanadium concentration was 11.0 wt ppm. In addition, the yield of the raw material oil of asphalt (bitumen) M14A was 4.5 wt%.

Subsequently, a mixed oil of the deasphalted oil M13A and the vacuum gas oil M11A obtained was introduced into a reactor filled with a hydrogenation demetal catalyst and a hydrodehydration catalyst at a vol ratio of 1: 9, and hydrogenated demetallization and dehydration in the presence of hydrogen and the catalyst. Treatment (hydrogenation demetal and dehydration step 22A) was carried out to obtain HDMS refined oil M15A. Further, the treatment was conducted in the conditions of hydrogen partial pressure to 100 atm, (H ₂ / oil) ratio of 800 Nl / l, a LHSV 0.5 / hr, the reaction temperature was 375 ℃. The yield of the obtained HDMS refined oil M15A was 38.4 wt%, the sulfur concentration was 0.10 wt%, and the vanadium concentration was 0.9 wt ppm.

Next, in the obtained HDMS refined oil M15A, 22.7 wt% (relative to the crude oil) was mixed with the effluent oil M3A, and the gas turbine fuel having a yield of crude oil of 73.6 wt%, a sulfur concentration of 0.49 wt%, and a vanadium concentration of 0.28 wt ppm. Got. In addition, the remainder of the HDMS refined oil, i.e., 15.7 wt%, was used as raw material for fluid catalytic cracking (FCC) or hydrocracking (HCR) as it is.

According to the petroleum refining method of the present invention, a petroleum product (gas turbine fuel) having a vanadium (V) concentration of 0.5 wt ppm or less, for example, from heavy oil (heavy raw material oil) such as orinoco tar or low crude sulfur oil. And an intermediate petroleum product having a metal concentration (V + Ni) of 30 wt ppm or less, which is suitable as a fluid catalytic cracking (FCC) raw material or a hydrocracking (HCR) raw material, can be efficiently produced together.

Claims (26)

A petroleum refining method for refining crude oil to produce petroleum products including various intermediate petroleum products, A distillation separation process of distilling raw oil and separating the effluent oil and residual oil; At least a portion of the effluent oil obtained in the distillation separation step is subjected to hydrorefining treatment in the presence of hydrogen and a catalyst, and dehydrogenated to obtain dehydrogenated refined oil; A solvent removal step of solvent-removing the residual oil to obtain deasphalted oil as an extract and the remaining asphalt (bitumen); At least a part of the deasphalted oil in the presence of hydrogen and a catalyst for hydrodemetalization and deflow treatment to obtain a demetallized and deflow-refined HDMS refined oil; And a first mixing step of mixing a portion of the HDMS refined oil and at least a portion of the demineralized refined oil and obtaining one of the petroleum products. The method of claim 1, The petroleum product obtained in the first mixing process is a gas turbine fuel, The solvent removal step controls the extraction rate so that the extraction rate of vanadium in the deasphalted oil obtained in relation to vanadium in the residual oil as the feedstock is 20% or less, and in particular, the HDMS refined oil obtained by treating deasphalted oil in a hydrodemetalization / deflow process. The demetal-dehydration conditions are selected so that the vanadium concentration of 2 wt ppm or less and the sulfur concentration may be 0.5 wt% or less. The method of claim 1, The petroleum product obtained in the first mixing process is a gas turbine fuel, In the first mixing step, the mixing conditions are set such that the vanadium concentration of the gas turbine fuel is 0.5 wt ppm or less. The method of claim 1, The remainder of the said HDMS refined oil is an intermediate petroleum product as a raw material for fluid catalytic cracking or hydrocracking, The petroleum purification method characterized by the above-mentioned. A petroleum refining method for refining crude oil to produce petroleum products including various intermediate petroleum products, A distillation separation process of distilling the raw oil to separate the effluent oil and the residual oil; At least a portion of the effluent oil obtained in the distillation separation step is subjected to hydrorefining treatment in the presence of hydrogen and a catalyst, and dehydrogenated to obtain dehydrogenated refined oil; A solvent removal step of solvent-removing the residual oil to obtain deasphalted oil as the extract and remaining asphalt (bitumen); At least a part of the deasphalted oil in the presence of hydrogen and a catalyst, followed by a hydrodemetalization and deflow treatment to obtain a demetallized and deflow-refined HDMS refined oil; A vacuum distillation separation process of distilling the HDMS refined oil under reduced pressure distillation to separate the reduced pressure gas oil and a reduced pressure residual oil, And a second mixing step of mixing at least a portion of the vacuum gas oil and at least a portion of the demineralized refined oil to obtain one of the petroleum products. The method of claim 5, The petroleum product obtained in the second mixing process is a gas turbine fuel, The solvent removal step controls the extraction rate so that the extraction rate of vanadium in the deasphalted oil obtained with respect to vanadium in the resid as the feedstock is 30% or less, and the deasphalted oil is obtained by treating the deasphalted oil in a hydrodehydration / dehydration step. Demetal and deflow conditions are selected so that the vanadium concentration is 20 wt ppm or less and the sulfur concentration is 0.5 wt% or less, and the vanadium concentration of the vacuum gas oil obtained in the vacuum distillation separation process is 1 wt ppm or less. Petroleum Refining Method. The method of claim 5, The petroleum product obtained in the second mixing process is a gas turbine fuel, In the second mixing step, the mixing conditions are set such that the vanadium concentration of the gas turbine fuel is 0.5 wt ppm or less. The method of claim 5, A petroleum refining method, wherein the vacuum gas oil obtained by distilling at least a portion of the HDMS refined oil under reduced pressure is an intermediate petroleum product as a raw material for fluid catalytic cracking or hydrocracking. A petroleum refining method for refining crude oil to produce petroleum products including various intermediate petroleum products, A distillation separation process of distilling the raw oil to separate the effluent oil and the residual oil; At least a portion of the effluent oil obtained in the distillation separation step is subjected to hydrorefining treatment in the presence of hydrogen and a catalyst, and dehydrogenated to obtain dehydrogenated refined oil; A vacuum distillation separation process of distilling the residual oil under reduced pressure distillation to separate the vacuum oil and the vacuum residue; A solvent removal treatment step of performing solvent removal treatment on the vacuum residue to obtain deasphalted oil as an extract and remaining asphalt (bitumen); A hydrogenation demetalization and degassing step of mixing the reduced-pressure diesel oil with deasphalted oil and subjecting the mixed oil to hydrodemetalization and deflow treatment in the presence of hydrogen and a catalyst to obtain demetalization and deflow-refined HDMS refined oil; And a third mixing step of mixing a portion of the HDMS refined oil and at least a portion of the demineralized refined oil and obtaining one of the petroleum products. The method of claim 9, The petroleum product obtained in the third mixing process is a gas turbine fuel, The solvent removal step controls the extraction rate so that the extraction rate of vanadium in the deasphalted oil obtained in relation to vanadium in the residual oil as the feedstock is 15% or less, and in particular, the vanadium concentration of the HDMS refined oil is 2 wt ppm or less, and the sulfur concentration is 0.5. The petroleum refining method characterized by selecting the conditions of the said demetal-dehydration process so that it may become wt% or less. The method of claim 1, The petroleum product obtained in the third mixing process is a gas turbine fuel, In the third mixing step, the mixing conditions are set such that the vanadium concentration of the gas turbine fuel is 0.5 wt ppm or less. The method of claim 9, The remainder of the said HDMS refined oil is an intermediate petroleum product as a raw material for fluid catalytic cracking or hydrocracking, The petroleum refining method characterized by the above-mentioned. The method according to claim 1, 5 or 9, The raw material is a petroleum refining method, characterized in that the API degree is 20 or less heavy oil. A petroleum refining method for refining crude oil to produce petroleum products including various intermediate petroleum products, A distillation separation process of distilling the raw oil to separate the effluent oil and the residual oil; A solvent removal treatment step of removing the residual oil obtained in the distillation separation step to obtain a deasphalted oil as the extract and the remaining asphalt (bitumen); At least a part of the deasphalted oil in the presence of hydrogen and a catalyst, followed by a hydrodemetalization and deflow treatment to obtain a demetallized and deflow-refined HDMS refined oil; And a fourth mixing step of mixing a portion of the HDMS refined oil and at least a portion of the effluent oil to obtain one of the petroleum products. The method of claim 14, The petroleum product obtained in the fourth mixing process is a gas turbine fuel, The extraction rate in the solvent removal process is controlled so that the vanadium concentration in the deasphalted oil is 25 wt ppm or less, and in particular, the hydrodehydration is carried out such that the vanadium concentration of the HDMS refined oil is 2 wt ppm or less and the sulfur concentration is 0.5 wt% or less. The petroleum refining method characterized by selecting metal-dehydration treatment conditions. The method of claim 14, The petroleum product obtained in the fourth mixing process is a gas turbine fuel, In the fourth mixing step, the mixing conditions are set such that the vanadium concentration of the gas turbine fuel is 0.5 wt ppm or less. The method of claim 14, The remainder of the said HDMS refined oil is an intermediate petroleum product as a raw material for fluid catalytic cracking or hydrocracking, The petroleum refining method characterized by the above-mentioned. A petroleum refining method for refining crude oil to produce petroleum products including various intermediate petroleum products, A distillation separation process of distilling the raw oil to separate the effluent oil and the residual oil; A solvent removal treatment step of removing the residual oil obtained in the distillation separation step to obtain a deasphalted oil as the extract and the remaining asphalt (bitumen); At least a part of the deasphalted oil in the presence of hydrogen and a catalyst, followed by a hydrodemetalization and deflow treatment to obtain a demetallized and deflow-refined HDMS refined oil; A reduced pressure distillation process of distilling the HDMS refined oil under reduced pressure to separate the reduced pressure gas oil and the reduced pressure oil; And a fifth mixing step of mixing at least a portion of the reduced pressure diesel oil and at least a portion of the outflow oil to obtain one of the petroleum products. The method of claim 18, The petroleum product obtained in the fifth mixing process is a gas turbine fuel, The extraction rate in the solvent removal process is controlled so that the vanadium concentration in the deasphalted oil is 50 wt ppm or less, and the hydrogenated demetallization is performed so that the vanadium concentration of the HDMS refined oil is 20 wt ppm or less and the sulfur concentration is 0.5 wt% or less. -The petroleum refining method characterized by selecting deflow treatment conditions and setting the vanadium concentration of the vacuum gas oil obtained in the vacuum distillation separation process to 1 wt ppm or less. The method of claim 18, The petroleum product obtained in the fifth mixing process is a gas turbine fuel, In the fifth mixing step, the mixing conditions are set such that the vanadium concentration of the gas turbine fuel is 0.5 wt ppm or less. The method of claim 18, The petroleum refining method characterized by using the vacuum gas oil obtained by distilling at least one part of the said HDMS refined oil under reduced pressure as an intermediate petroleum product as a raw material for fluid catalytic cracking or hydrocracking. A petroleum refining method for refining crude oil to produce petroleum products including various intermediate petroleum products, A distillation separation process of distilling the raw oil to separate the effluent oil and the residual oil; A vacuum distillation separation step of distilling the residual oil obtained in the distillation separation process under reduced pressure to separate the vacuum gas oil and the vacuum residue, A solvent removal treatment step of performing solvent removal treatment on the vacuum residue to obtain deasphalted oil as an extract and remaining asphalt (bitumen); A hydrogenation demetalization and degassing step of mixing the reduced-pressure diesel oil with deasphalted oil and subjecting the mixed oil to hydrodemetalization and deflow treatment in the presence of hydrogen and a catalyst to obtain demetalization and deflow-refined HDMS refined oil; And a sixth mixing step of mixing a portion of the HDMS refined oil and at least a portion of the effluent oil to obtain one of the petroleum products. The method of claim 22, The petroleum product obtained in the sixth mixing process is a gas turbine fuel, The extraction rate in the solvent removal process is controlled so that the vanadium concentration in the deasphalted oil is 70 wt ppm or less, and in particular, the hydrodehydration is performed such that the vanadium concentration of the HDMS refined oil is 2 wt ppm or less and the sulfur concentration is 0.5 wt% or less. The petroleum refining method characterized by selecting metal-dehydration treatment conditions. The method of claim 22, The petroleum product obtained in the sixth mixing process is a gas turbine fuel, In the sixth mixing step, the mixing conditions are set such that the vanadium concentration of the gas turbine fuel is 0.5 wt ppm or less. The method of claim 22, The remainder of the said HDMS refined oil is an intermediate petroleum product as a raw material for fluid catalytic cracking or hydrocracking, The petroleum refining method characterized by the above-mentioned. The method according to claim 14, 18 or 22, The crude oil is a petroleum refining method, characterized in that the sulfur concentration is low sulfur crude oil of 2.0 wt ppm or less.