JPH0782573A - Method and apparatus for treating petroleum - Google Patents

Abstract

PURPOSE:To treat petroleum at a low cost with a simple apparatus by distilling a crude oil under the normal pressure to separate it into a residual oil and a distillate oil and hydrogenating the distillate oil collectively with one hydrogenation apparatus. CONSTITUTION:A crude oil pretreated, e.g. dewatered and desalted, is fed to a rough-distillation apparatus 11, distilled under the normal pressure, and thus separated into a light oil, a distillate oil comprising fractions more volatile than the light oil, and a residue (a normal-pressure residual oil). The distillate oil is collectively fed to a hydrogenation apparatus 12 and where brought into contact with hydrogen in the presence of a catalyst to be subjected to hydrogenation such as desulfurization. The resulting refined oil is fractionated into a refined light oil, a refined kerosene, a refined heavy naphtha, a refined light naphtha, a refined LP gas, and an off-gas (a light gas). Thus, the construction of a petroleum refinery system is greatly simplified and the construction cost and equipment space are greatly reduced in comparison with the conventional method wherein a crude oil is distilled and separated into various fractions and then each fraction is hydrogenated separately.

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a treatment method and apparatus for separating light oil, kerosene, heavy naphtha, light naphtha, LP gas, and light gas fractions from crude oil and hydrotreating them.

[0002]

2. Description of the Related Art FIG. 8 is a diagram for explaining a conventional general oil making process. The crude oil is subjected to pretreatments such as dehydration and desalting and then supplied to the atmospheric distillation apparatus 1. And atmospheric distillation unit 1
In, the crude oil is distilled under atmospheric pressure to separate into light gas, LP gas, light naphtha, heavy naphtha, kerosene, light oil and residual oil fractions. After separation, the light gas (off-gas) having the lowest boiling point is combined with a gas purified from another processing device to separate the acid gas in the amine processing device 2 to be used as a fuel gas. The acid gas is sent to the sulfur recovery device 3 to recover sulfur. The separated LP gas is used as a product LP gas after impurities are removed by the LP gas processing device 4. The light naphtha fraction is subjected to simple treatment such as sweetening treatment in the light naphtha treatment device 5 to be blended with gasoline. The heavy naphtha fraction is sent to the hydrotreating device 6, hydrotreated in the presence of a catalyst, and then sent to the catalytic reforming device 7, where it is isomerized or aromatized to give gasoline. The kerosene fraction is sent to the kerosene processing device 8 to be refined into kerosene. The light oil fraction is sent to a light oil hydrotreating apparatus 9, where it is hydrotreated in the presence of a catalyst to remove impurities, and then made into light oil. The crude naphtha produced here is returned to the atmospheric distillation apparatus 1. The residual oil remaining at the bottom of the distillation apparatus 1 is
It is taken out from the distillation apparatus 1 and used as a blending material for heavy oil, or sent to a vacuum distillation apparatus and distilled under reduced pressure to separate a vacuum distillation oil which is a raw material for producing light oil. As described above, in the conventional method, regardless of the amount of crude oil treated, the crude oil is uniformly divided into each fraction in the distillation column, and each is individually hydrotreated.

[0003]

However, in the conventional petroleum processing method, since the crude oil is divided into each fraction in the distillation column and each of them is individually hydrotreated, complicated equipment is unavoidable. However, there is a problem in that the device structure becomes complicated and the construction cost becomes high. In particular, when the amount of crude oil processed is small, it has been desired to develop a processing method with a more compact device configuration and low cost.

The present invention has been made in view of the above circumstances, and the construction of the equipment of a petroleum processing system is simplified, the construction cost and the installation space can be reduced, and the construction of the equipment can be improved even when the amount of crude oil processed is small. It is an object of the present invention to provide a new petroleum processing method and device, which are expected to be compact.

[0005]

A method for treating petroleum according to the present invention is a method in which crude oil is distilled under atmospheric pressure to separate a residual oil and a distillate oil, and the distillate oil is collectively treated with hydrogen in the same hydrotreating apparatus. The feature is that it is processed. The hydrogenated refined oil may be distilled and separated into light oil, kerosene, heavy naphtha, light naphtha, LP gas, and light gas fractions. Preferably, the separated heavy naphtha is supplied to the catalytic reformer to be converted into gasoline, and at the same time, hydrogen having a purity of 75% or more is recovered from the light gas produced as a by-product, and the hydrogen is treated by the hydrotreating apparatus. Supply to. Further, the atmospheric residual oil is supplied to a vacuum distillation apparatus for vacuum distillation, and the vacuum gas oil separated is subjected to hydrotreating together with the distillate in atmospheric distillation in the same hydrotreating apparatus. good. As the hydrotreating apparatus used in this petroleum processing method, it is possible to select from a gas-liquid downward cocurrent reactor, a gas-liquid countercurrent reactor, and a gas-liquid upward cocurrent reactor. desirable. More preferred are a gas-liquid downward co-current type reactor and a gas-liquid upward co-current type reactor equipped with an intermediate gas-liquid separation means for performing gas-liquid separation in the middle part of the reactor. Furthermore, in this petroleum treatment method, a part of the hydrotreated refined oil may be returned to the inlet of the hydrotreating apparatus. The conditions for the hydrotreatment are that the pressure is 20 to 80 kg / cm ² G, preferably 3
0 to 70 kg / cm ² G, temperature is 300 to 400 ° C., preferably 320 to 380 ° C., H ₂ / oil ratio is 50 to 200.
Nl / l, preferably 70-150 Nl / l, LHSV
Is preferably selected in the range of 0.1 to 5, preferably 1 to 4.

[0006] The petroleum processing apparatus of the present invention comprises an atmospheric distillation apparatus for distilling crude oil under atmospheric pressure to separate it into a residual oil and a distillate oil, and a distillate oil separated by the atmospheric distillation apparatus. And a hydrotreating device for hydrotreating. The petroleum treatment apparatus of the present invention is provided with a distiller for separating refined oil treated by the hydrotreating apparatus into light oil, kerosene, heavy naphtha, light naphtha, LP gas, and light gas fractions. As good as. Further, in each of the separated fractions, a catalytic reformer for converting heavy naphtha into gasoline and a purity of 7 by-produced in the catalytic reformer are used.
A by-product hydrogen supply line for supplying 5% or more hydrogen to the hydrotreating apparatus may be provided, and a vacuum distillation apparatus for distilling the residual oil under reduced pressure to collect vacuum gas oil from the residual oil. Alternatively, the vacuum gas oil collected by the vacuum distillation apparatus may be mixed with the distillate oil from the atmospheric distillation apparatus to supply a vacuum gas oil supply line to the hydrotreating apparatus. In the petroleum treatment apparatus of the present invention, the hydrotreating apparatus is one of a gas-liquid downward cocurrent reactor, a gas-liquid countercurrent reactor, and a gas-liquid upward cocurrent reactor. Is desirable. Among these, the gas-liquid downward co-current reactor and the gas-liquid upward co-current reactor are
Those equipped with an intermediate gas-liquid separation means for performing gas-liquid separation in the middle part of the reactor are preferable. Further, the petroleum processing apparatus may be configured to include refined oil returning means for returning a part of the refined oil processed by the hydrotreating apparatus to the inlet of the hydrotreating apparatus.

[0007]

In the present invention, crude oil is distilled under atmospheric pressure to separate it into a residual oil and a distillate oil, and the distillate oil is collectively hydrotreated in the same hydrotreating apparatus to distill the crude oil. Compared with the case where hydrofraction is performed for each fraction after fine fractionation, the device configuration of the refinery is simplified and the construction cost and installation space can be reduced. Further, even when the amount of crude oil processed is small, the apparatus configuration can be made more compact. In the present invention, crude oil is distilled under atmospheric pressure to separate a residual oil and a distillate oil.
As this distillate oil, all parts (light oil, kerosene, naphtha, LP gas, light gas) excluding atmospheric residual oil may be obtained in the form of one distillate oil, or a plurality of distillate oils may be obtained. It can also be obtained in divided form in oil. For example, during atmospheric distillation, a gas oil fraction and a fraction having a boiling point lower than that can be obtained as separate distillate oils. Further, a distillate that does not require hydrotreating and a distillate containing a distillate that requires hydrotreating may be separately obtained. For example, light gas as a fraction that does not require hydrotreatment is separated and removed during atmospheric distillation to obtain distillate oil that does not contain light gas, and to introduce this into the hydrotreatment device. Is also good. Further, when distillate oil containing light gas is obtained during atmospheric distillation, it is possible to separate and remove light gas before introducing it into the hydrotreating device to obtain distillate oil containing no light gas. . When distillate oil is obtained by dividing it into a plurality of distillate oils, it is preferable that the number of distillate oils is smaller because the distillation apparatus configuration is simplified. In the present invention, among the above distillates, that is, those obtained in the form of one distillate or those obtained in the form of being divided into a plurality of distillates, a distillate containing a fraction requiring hydrotreatment. The oil is introduced into the same hydrotreating device, and is hydrotreated collectively. At this time, a fraction obtained in the atmospheric distillation that does not require hydrotreating can also be introduced into the hydrotreating apparatus. The conditions for the hydrotreatment are that the pressure is 20 to 80 kg / cm ² G, preferably 30.
˜70 kg / cm ² G, temperature 300 to 400 ° C., preferably 320 to 380 ° C., H ₂ / oil ratio 50 to 200 N
1 / l, preferably 70 to 150 Nl / l, and LHSV is preferably selected in the range of 0.1 to 5, preferably 1 to 4. Any hydrogen-containing gas may be used as the hydrogen source, and those having a purity of 60% or more are preferable. As the catalyst for hydrotreating, any catalyst that can be used for hydrotreating may be used, and for example, Co—Mo type, Ni—Mo type and the like are usually used.

[0008]

DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention will be described in detail below with reference to the drawings. FIG. 1 is a diagram for explaining an example of the petroleum processing method of the present invention. In this petroleum treatment method, crude oil that has been subjected to pretreatments such as dehydration and desalting is first sent to a crude distillation device 11, where crude oil is distilled under atmospheric pressure, and light oil and distillates having a boiling point lower than that (kerosene, naphtha, etc. , LP gas, light gas) and the residue (atmospheric pressure residual oil) are separated.

The distillate oil separated in the crude distillation unit 11 is sent to the hydrotreating unit 12 in a lump, and is brought into contact with hydrogen in the presence of a catalyst to perform hydrotreating such as desulfurization of the distillate oil. At the same time, the hydrogenated refined oil is fractionally distilled to produce refined gas oil, refined kerosene, refined heavy naphtha, refined light naphtha,
Separate into purified LP gas and offgas (light gas) fractions. As the hydrotreating device 12, a gas-liquid downward cocurrent reactor, a gas-liquid countercurrent reactor, a gas-liquid upward cocurrent reactor,
Furthermore, it is desirable to select and use from reactors and the like incorporating an intermediate gas-liquid separation type. As hydrogen (H ₂ ) used in the hydrotreating process, hydrogen produced as a by-product from the catalytic reforming device 7 that performs the catalytic reforming process of the purified heavy naphtha can be used. In this case, the purity of hydrogen by-produced is preferably 75% or more, and more preferably 80% or more. In addition, when it is not necessary to hydrotreate the entire amount of gas oil, only a part of the gas oil fraction separated from the crude distillation apparatus 11 is sent to the hydroprocessing apparatus 12 for hydroprocessing, and after hydroprocessing, The refined gas oil obtained may be mixed with a gas oil fraction which is not hydrotreated.

FIG. 2 shows a gas-liquid downward co-current reactor as a first example of the hydrotreating apparatus. This apparatus includes a reactor 21 filled with a hydrogenation catalyst 20, a gas-liquid separator 25, and a fractionator 23 as main components. In order to carry out hydrotreating and fractional distillation of distillate oil using this device, distillate oil, for example, gas oil and a fraction having a boiling point lower than that, and hydrogen are supplied from the upper side of the reactor 20. ,
While distilling these gas and liquid downwards, the distillate oil is hydrogenated and purified at a constant temperature and pressure. Then, the refined oil and the gas phase are taken out from the bottom of the reactor 21 and sent to the gas-liquid separator 25, where the refined oil and the gas phase (unreacted hydrogen, generated gas, etc.) are separated, and the separated refined oil is separated. While being sent to the fractionator 23, the separated gas phase part can be separated and removed from the produced gas such as hydrogen sulfide if necessary, and then returned to the reactor 21 for recycling. The refined oil sent to the fractionator 23 is subjected to atmospheric distillation here to separate into light oil, kerosene, naphtha, LP gas and off gas (light gas). If necessary, the separated light oil may be returned to the reactor 21 again for hydrotreatment.

FIG. 3 shows, as a second example of the hydrotreating apparatus, a reactor incorporating an intermediate gas-liquid separating means in a gas-liquid upward co-current type. This apparatus is similar to the hydrotreating apparatus shown in FIG. 2 and has a reactor 21 in which hydrogenation catalysts 20 are arranged in multiple stages.
And an intermediate gas-liquid separator 22, a gas-liquid separator 25, and a fractionator (not shown). To hydrotreat distillate oil using this apparatus, distillate oil and hydrogen are supplied from the bottom of the reactor 21, and the distillate oil is hydrogenated at a constant temperature and pressure while flowing these upwards. And purify. Then, the refined oil discharged from the lower catalyst layer is sent to the intermediate gas-liquid separator 22, where it is separated into a gas phase and a liquid phase, and the gas phase further passes through the upper catalyst phase and is taken out from the upper part of the reactor and cooled. It is sent to the gas-liquid separator 25 and separated into off gas and refined oil. The liquid phase exiting the intermediate gas-liquid separator 22 and the refined oil from the gas-liquid separator 25 are sent to the fractionator separately or in combination and are sent to light oil, kerosene, naphtha, L
It is separated into each fraction such as P gas and off gas.

FIG. 4 shows, as a third example of the hydrotreating apparatus, a reactor incorporating an intermediate gas-liquid separating means in a gas-liquid downward co-current type. This apparatus is similar to the hydrotreating apparatus shown in FIG. 2 and has a reactor 21 in which hydrogenation catalysts 20 are arranged in multiple stages, an intermediate gas-liquid separator 22, a gas-liquid separator 25, and a fractional distillation not shown. And a container. To hydrotreat distillate oil using this apparatus, distillate oil and hydrogen are supplied from the upper part of the reactor 21, and the distillate oil is hydrogenated at a constant temperature and pressure while flowing these downwards. And purify. Then, the gas-liquid mixture is taken out from the bottom of the upper catalyst layer and sent to the intermediate gas-liquid separator 22, where it is separated into a gas phase and a liquid phase, and the gas phase exiting the intermediate gas-liquid separator 22 is a gas-liquid after cooling. It is sent to the separator 25 and separated into refined oil and off-gas. Intermediate gas-liquid separator
The liquid phase separated in 22 is made to flow down to the lower catalyst layer, and hydrogenation treatment is performed again. The refined oil taken out from the bottom of the reactor 21 and the refined oil taken out from the gas-liquid separator 25 are separately or combined and sent to a fractionator to be separated into each fraction such as light oil, kerosene, naphtha, and LP gas. It

FIG. 5 illustrates a gas-liquid countercurrent type reactor which is a fourth example of the hydrotreating apparatus. This device
A reactor 21 in which the hydrogenation catalyst 20 is arranged in multiple stages, a cooler 24,
A gas-liquid separator 25, a hydrogen sulfide removing device 26, a circulation compressor 27, and a fractionator (not shown) are provided. To hydrotreate the raw material distillate oil using this apparatus, the distillate oil is supplied to the intermediate portion between the upper catalyst layer and the lower catalyst layer, and hydrogen is supplied from the bottom of the reactor 21.
The distillate oil is separated into a gas phase consisting of a gasified low-boiling point component and a liquid phase consisting of a high-boiling point component in the above intermediate part, and the liquid phase is flowing down through the lower catalyst layer and in countercurrent contact with hydrogen. It is hydrotreated, and while the gas phase is mixed with hydrogen and flows upward in the upper catalyst layer, it is hydrotreated and taken out from the upper part of the reactor. In this gas phase, low boiling point components in the distillate,
It contains unreacted hydrogen and generated gas, which are sent to a cooler 24 to be cooled to liquefy low-boiling components and then separated into a liquid phase (low-boiling components) and a gas phase in a gas-liquid separator 25. To separate.
The liquid phase taken out from the gas-liquid separator 25 and the refined oil taken out from the bottom of the reactor 21 are separately or combined and sent to the fractionator 23, where light oil, kerosene, naphtha, LP gas and off gas (light gas ) Etc. are separated into each fraction. The gas phase separated by the gas-liquid separator 25 is sent to a hydrogen sulfide removal device 26 equipped with a PSA (Pressure swing adsorption) device or the like to remove hydrogen sulfide in the gas phase, and then the pressure is increased by a circulation compressor 27 to remove hydrogen. The recycled gas is returned to the reactor 21 and circulated. In this equipment, distillate oil is separated into a gas phase (low boiling point component) and a liquid phase (high boiling point component), and the high boiling point fraction containing a large amount of sulfur compounds that are difficult to decompose is flowed down while contacting with hydrogen in countercurrent. To hydrogenate strongly, while hydrogen is mixed with a low boiling point component that is easy to hydrogenate and flows upward to hydrogenate, so a distillate that contains multiple components with different boiling points and different sulfur decomposability The oil can be hydrogenated very efficiently.

FIG. 6 exemplifies a reactor in which an intermediate gas-liquid separation means is incorporated in a gas-liquid downward co-current type as a hydrotreating apparatus suitable for further refining a relatively light fraction. In this device, distillate oil and hydrogen are supplied from the upper part, and after performing the first treatment in the upper catalyst layer, the fluid flowing out from the bottom part of the catalyst layer is guided to the intermediate gas-liquid separator 22, and the gas phase is separated. And liquid phase. This liquid phase is a refined oil. On the other hand, the gas phase part is supplied again to the lower catalyst layer of the reactor 21 to perform further hydrogenation treatment. The fluid leaving the lower catalyst layer is cooled and then introduced into a gas-liquid separator 25 to be separated into a gas phase and a liquid phase. The gas phase is used for fuel or hydrogen recovery, and the liquid phase is refined oil. The refined oil taken out from the intermediate gas-liquid separator 22 and the refined oil taken out from the gas-liquid separator 25 are separately or combined and sent to a fractionator.

FIG. 7 exemplifies a gas-liquid downward cocurrent flow reactor as a hydrotreating device which makes purification of a relatively light fraction more effective. In this device, distillate oil is used. A gas-liquid separator 25A provided upstream of a reactor 21 having a plurality of catalyst layers 20 separates a gas phase and a liquid phase, supplies the gas phase from the upper portion of the reactor, and supplies the liquid phase to an intermediate portion of the catalyst layer. To do. The gas-liquid refined oil that emerges from the bottom of the reactor is led to the first gas-liquid separator 25B, where it is separated into a gas phase and a liquid phase, and a part of the separated gas phase is reacted as shown by the broken line arrow in the figure. After returning to the upper part of the vessel and cooling some other gas, it is led to the second gas-liquid separator 25C. The liquid phase exiting the first gas-liquid separator 25B is cooled and then sent to the fractionator either confluent with the liquid phase from the second gas-liquid separator 25C or separately. It is also possible to simply cool the fluid leaving the reactor 21 and then separate it into off gas and refined oil with a gas-liquid separator.

As shown in FIG. 1, from the hydrotreating apparatus 12 through the hydrotreating and fractionating treatments as described above,
Refined light oil, refined heavy naphtha, refined light naphtha, refined LP
Gas and off-gas fractions are obtained. The off-gas separates the acid gas in the amine processing device 2 to be used as a fuel gas, while sending the acid gas to the sulfur recovery device 3 to recover sulfur. The purified LP gas is used as a product LP gas as it is.
The refined light naphtha can be directly blended with gasoline, and may be subjected to reforming treatment or sweetening treatment as necessary. The refined heavy naphtha is sent to the catalytic reforming device 7, where it is isomerized or aromatized and then blended into gasoline. The hydrogen by-produced in the catalytic reforming device 7 is sent to the hydrotreating device 12 to be used as hydrogen for hydrogenation, and the LP gas component by-produced is returned to the hydrotreating device 12 or the hydrotreating device 12. It can also be mixed with the purified LP gas obtained from 12. Further, the refined kerosene can be directly used as a product kerosene. The refined gas oil can be directly used as the product gas oil.

The residue (residual oil) remaining at the bottom of the crude distillation apparatus 11 is taken out from the crude distillation apparatus 11 and used as a heavy oil blending material as it is, or sent to a vacuum distillation apparatus for vacuum distillation and vacuum distillation. Separate the oil. At least a part of the vacuum distillate oil obtained here may be mixed with the distillate oil from the crude distillation apparatus 11 and hydrotreated in the hydrotreating apparatus 12.

In the above-mentioned petroleum treatment method, crude oil is subjected to atmospheric distillation to separate it into a residual oil and a distillate oil, and the distillate oil is collectively hydrotreated in the same hydrotreating apparatus. Compared with the case of distilling and finely fractionating and then hydrotreating each fraction, the equipment configuration of the refinery is simplified, and the construction cost and installation space can be reduced. Further, even when the amount of crude oil processed is small, the apparatus configuration can be made more compact.

(Experimental example) -Comparative example: Petroleum treatment by conventional method Based on the treatment system shown in FIG. 8, crude oil was distilled and separated into each fraction by an atmospheric distillation apparatus, and then hydrogenated for each fraction. It was supplied to a processing apparatus and hydrorefined. The properties of each fraction are as follows. Properties of crude oil: Arabian light and heavy (50vol /
50vol), specific gravity 0.8618, sulfur concentration 1.818wt%. Distillation properties of each fraction, yield: Table 1.

[0020]

[Table 1]

The main reaction conditions for the hydrogenation reaction test of each separated fraction were as follows. Catalyst: Commercially available (Catalyst Kasei Co., Ltd.) Co / Mo-based catalyst Reactor: Inner diameter 8 mm x length 6000 mm Filled catalyst amount: 96 cc Reactor type: Downward cocurrent hydrogen purity: 70% Hydrogen purification of each fraction Table 2 shows the reaction conditions and reaction results.

[0022]

[Table 2]

Example 1: Batch hydrogenation treatment of continuous fraction of light naphtha to light oil Using the continuous fraction from light naphtha to light oil (true boiling point C5 to 360 ° C.) shown in the preceding comparative example as a raw material, The same reactor as in Comparative Example 1 was used, and the continuous fraction was hydrotreated in the same reactor at once. The reaction conditions were as follows. Pressure: 40 kg / cm ² G Temperature: 330 ° C. H ₂ / Oil ratio: 100 Nm ³ / kiloliter LHSV: 3.1 1 / hr Under the above conditions, the continuous distillates are collectively hydrotreated, and the refined oil after the treatment is treated. The mixture was transferred to a fractionator and subjected to atmospheric distillation to distill and separate into light naphtha, heavy naphtha, kerosene and light oil fractions, and the residual sulfur concentration of each of these fractions was measured. The residual sulfur concentration of each fraction was light naphtha: 0.1 wtppm, heavy naphtha: 0.3 wtppm, kerosene: 0.001 wt%, and light oil: 0.20 wt%. It was as good as that. From these results, it was demonstrated that according to the present invention, the configuration of the petroleum refining apparatus can be greatly simplified, and the same hydrotreatment effect as the conventional one can be obtained.

Example 2: Batch hydrotreatment of continuous fraction of light naphtha to light oil Light naphtha under the same conditions as in Example 1 except that LHSV was set to 1.2 1 / hr and the amount of charged catalyst was set to 250 cc. ~ A batch distillate of light oil was subjected to a batch hydrotreatment. The residual sulfur concentration of each fraction was light naphtha: 0.1 wtppm or less, heavy naphtha: 0.1 wtppm or less, kerosene: 0.0003 wt%, light oil: 0.05 wt%, which was a good result.

Example 3: Collective hydrogenation treatment by gas-liquid countercurrent reactor Using the gas-liquid countercurrent reactor shown in FIG. 5 as a reactor, the same feedstock as in Example 1 (light naphtha to light oil) was used. Continuous distillates up to) were processed. The catalyst layer in the reactor is divided into upper and lower layers, and the feed oil (continuous fraction) is supplied between the upper catalyst layer and the lower catalyst layer, and hydrogen is supplied from the bottom of the reactor to collectively feed oil. It was hydrotreated. The reaction conditions were as follows. Upper catalyst amount: 40 cc Lower catalyst amount: 60 cc Pressure: 40 kg / cm ² G Temperature: 330 ° C. H ₂ / oil ratio: 100 Nm ³ / kiloliter LHSV: 3.1 1 / hr Purified oil after hydrogenation is fractionated The mixture was transferred to a vessel and subjected to atmospheric distillation to distill and separate into light naphtha, heavy naphtha, kerosene and light oil fractions, and the residual sulfur concentration of each of these fractions was measured. The residual sulfur concentration of each fraction was light naphtha: 0.1 wtppm or less, heavy naphtha: 0.1 wtppm or less, kerosene: 0.001 wt%, light oil: 0.15 wt%.

Example 4: Batch desulfurization treatment of LP gas to light oil The treatment was carried out under the same conditions as in Example 1 except that LP gas was added. However H ₂ / oil ratio, the feed amount of calculation based LHSV is light naphtha-gas oil (LP gas is excluded). The residual sulfur concentration of each fraction was light naphtha: 0.1 wtppm or less, heavy naphtha: 0.4 wtppm or less, kerosene: 0.001 wt%, light oil: 0.22 wt%.

[0027]

According to the present invention having the above-mentioned constitution,
It has the following effects. In the present invention, crude oil is subjected to atmospheric distillation to separate it into a residual oil and a distillate oil, and the distillate oil is collectively hydrotreated in the same hydrotreating apparatus to distill the crude oil and finely fractionate it. After that, as compared with the case where hydrotreating is performed for each fraction, the device configuration of the oil refining system can be greatly simplified, and construction cost and installation space can be reduced. Further, in the conventional method of performing hydrotreating for each fraction, maintenance of each hydrotreating device such as catalyst exchange has to be performed separately, and a lot of various equipment such as piping for that has been required, In the present invention, since the distillate oil is collectively hydrotreated by the same hydrotreating apparatus, the maintenance can be performed at one time, and the auxiliary equipment for the maintenance can be greatly simplified, and the maintenance can be performed easily. Since the number of times is reduced, it is possible to operate the oil refining plant efficiently. Further, as a petroleum treatment apparatus of the present invention, an atmospheric distillation apparatus for distilling crude oil under atmospheric pressure to separate a residual oil and a distillate oil, and a distillate oil separated by the atmospheric distillation apparatus are collectively hydrogenated. In addition to hydrotreating equipment for processing, refined oil treated by hydrotreating equipment is used as diesel oil, kerosene, heavy naphtha,
A fractionator for separating light naphtha, LP gas, and light gas into respective fractions, a catalytic reformer for converting heavy naphtha into gasoline from the separated fractions, and a by-product of the catalytic reformer. By providing a by-product hydrogen supply line for supplying hydrogen having a purity of 75% or more to the hydrotreating device, refined oil and gasoline of each of the above fractions can be produced, and the by-product hydrogen is hydrotreating device. Therefore, the cost of hydrogen gas used in the hydrotreating apparatus can be reduced. Further, a vacuum distillation apparatus for distilling the residual oil under reduced pressure to collect vacuum gas oil from the residual oil, and a vacuum gas oil collected by the vacuum distillation apparatus are mixed with distillate oil from the atmospheric distillation apparatus for hydrotreatment. By adopting the configuration provided with the reduced pressure gas oil supply line for supplying to the apparatus, the ratio of distillate oil can be increased and the utilization efficiency of crude oil can be improved. When a gas-liquid countercurrent reactor is used as the hydrotreating device, distillate oil is supplied to the middle part of the upper and lower catalyst phases of this reactor, and the distillate oil is put into the gas phase (low boiling point). (Distillate) and liquid phase (high-boiling fraction) are separated, and the high-boiling fraction containing a large amount of sulfur compounds that are difficult to decompose is flowed down and brought into contact with hydrogen in countercurrent to strongly hydrogenate, while hydrogenating It is possible to hydrogenate distillate oil containing multiple components with different boiling points and different decomposability of sulfur content very efficiently because hydrogen is mixed with low boiling point components and hydrogen is flown upward. it can. When a gas-liquid downward co-current type reactor or a gas-liquid upward co-current type reactor equipped with an intermediate gas-liquid separation means for performing gas-liquid separation in the middle part of the reactor is used as the hydrotreating device In this case, distillate oil may be taken out in the middle part of these reactors to separate gas-liquid, one of the separated gas phase and liquid phase may be taken out, and the other may be supplied to the reactor again for processing. It will be possible. For this reason, the distillate oil containing a plurality of components having different boiling points and different sulfur decomposability can be hydrogenated extremely efficiently and can flexibly meet the product specifications required for each fraction. Further, in the petroleum processing apparatus, a refined oil returning means for returning a part of the refined oil processed by the hydrotreating apparatus to the inlet of the hydroprocessing apparatus is provided, and the desired fraction is hydrotreated again. With such a constitution, even when a further purification treatment is required for a specific fraction, the object can be easily achieved.

[Brief description of drawings]

FIG. 1 is a process chart for explaining an example of a petroleum treatment method of the present invention.

FIG. 2 is a configuration diagram showing a first example of a hydrotreating apparatus suitable for the method of the present invention.

FIG. 3 is a configuration diagram showing a second example of a hydrotreating apparatus suitable for the method of the present invention.

FIG. 4 is a configuration diagram showing a third example of a suitable hydrotreating apparatus in the method of the present invention.

FIG. 5 is a configuration diagram showing a fourth example of a suitable hydrotreating apparatus in the method of the present invention.

FIG. 6 is a configuration diagram showing a fifth example of a suitable hydrotreating apparatus in the method of the present invention.

FIG. 7 is a configuration diagram showing a sixth example of a suitable hydrotreating apparatus in the method of the present invention.

FIG. 8 is a process chart for explaining a conventional petroleum treatment method.

[Explanation of symbols]

11 ... Coarse distillation apparatus (normal pressure distillation apparatus), 12 ... Hydrogenation apparatus, 20 ... Hydrogenation catalyst, 21 ... Reactor, 22
...... Intermediate gas-liquid separator, 23 …… Distiller, 24 …… Cooler, 25 …… Gas liquid separator, 26 …… Hydrogen sulfide removal device,
27 ... Circulation compressor.

 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Fujio Tsuchiya 1-1-14, Minami Sanrokusho, Yokohama-shi, Kanagawa JGC Corporation Yokohama Business Office (72) Inventor Makoto Inomata 1-14, Minami-sanroku, Yokohama 1 JGC Corporation Yokohama Office

Claims (16)

[Claims] 1. A method for treating petroleum, wherein crude oil is distilled under atmospheric pressure to separate into residual oil and distillate oil, and the distillate oil is collectively hydrotreated in the same hydrotreating apparatus. 2. A hydrotreated refined oil is distilled to obtain light oil,
The petroleum treatment method according to claim 1, wherein the kerosene, the heavy naphtha, the light naphtha, the LP gas, and the light gas are separated into respective fractions. 3. The separated heavy naphtha is supplied to a catalytic reformer to be converted into gasoline, and at the same time, hydrogen having a purity of 75% or more is recovered from light gas produced as a by-product, and the hydrogen is subjected to the hydrogenation. The oil processing method according to claim 2, wherein the oil is supplied to a processing device. 4. The atmospheric residual oil is supplied to a vacuum distillation apparatus for vacuum distillation, and the vacuum gas oil separated is hydrotreated together with the distillate obtained in atmospheric distillation in the same hydrotreating apparatus. The method for treating petroleum according to claim 1, wherein 5. The hydrotreating device is selected from a gas-liquid downward parallel flow type reactor, a gas-liquid countercurrent type reactor, and a gas-liquid upward parallel flow type reactor, and is used. Claims 1 to 4
The method for treating petroleum according to any one of the above. 6. The gas-liquid downward parallel flow type reactor and the gas-liquid upward parallel flow type reactor are provided with an intermediate gas-liquid separation means for performing gas-liquid separation in an intermediate portion of these reactors. Oil processing methods. 7. The petroleum treatment method according to claim 1, wherein a part of the hydrotreated refined oil is returned to the inlet of the hydrotreatment device. 8. A hydrotreating condition is that the pressure is 20 to 80 k.
g / cm ² G, temperature 300 to 400 ° C., H ₂ / oil ratio 50 to
The method for treating petroleum according to any one of claims 1 to 7, wherein the range is 200 Nl / l and LHSV 0.1-5. 9. The hydrotreating condition is that the pressure is 30 to 70 k.
g / cm ² G, temperature 320 to 380 ° C., H ₂ / oil ratio 70 to
The method for treating petroleum according to any one of claims 1 to 7, wherein the range is 150 Nl / l and LHSV1 to 4. 10. An atmospheric distillation apparatus for distilling crude oil under atmospheric pressure to separate it into a residual oil and a distillate oil, and a hydrotreatment for collectively hydrotreating the distillate oil separated by the atmospheric distillation apparatus. And a petroleum processing device. 11. A fractionator for separating refined oil treated by the hydrotreating apparatus into light oil, kerosene, heavy naphtha, light naphtha, LP gas, and light gas fractions. The petroleum treatment device according to claim 10. 12. A catalytic reformer for converting heavy naphtha of each of the separated fractions into gasoline, and a by-product for supplying hydrogen having a purity of 75% or more produced by the catalytic reformer to a hydrotreating apparatus. The petroleum processing apparatus according to claim 11, further comprising a raw hydrogen supply line. 13. A vacuum distillation apparatus for distilling the residual oil under reduced pressure to collect vacuum gas oil from the residual oil, and a vacuum gas oil collected by the vacuum distillation apparatus mixed with distillate oil from the atmospheric distillation apparatus. 11. The petroleum treatment apparatus according to claim 10, further comprising a reduced pressure gas oil supply line for supplying the hydrotreating apparatus. 14. The hydrotreating device is one of a gas-liquid downward co-current reactor, a gas-liquid counter-current reactor, and a gas-liquid upward co-current reactor. The petroleum treatment apparatus according to any one of claims 10 to 13. 15. A gas-liquid downward co-current type reactor and a gas-liquid upward co-current type reactor are equipped with an intermediate gas-liquid separation means for performing gas-liquid separation in an intermediate portion of these reactors. 15. The petroleum processing apparatus according to claim 14. 16. The refined oil returning means for returning a part of the refined oil processed by the hydrotreating apparatus to the inlet of the hydrotreating apparatus is provided. Any one of the petroleum processing equipment.