MXPA01004130A - Gas turbine fuel oil and production method thereof and power generation method - Google Patents

Abstract

Crude oil is separated into a light oil and a normal pressure residual oil by an atmospheric distillation and the light oil is brought into contact with a pressurized hydrogen in the presence of a catalyst to perform a first hydrogenation refining, a plurality of kinds of light oil obtained from an atmospheric distilling column being hydrogenation-refined collectively. The normal pressure residual oil is separated into a light component and a heavy component, the obtained light component is subjected to a second hydrogenation refining in the presence of a catalyst, the refined oil (light component) is mixed with the refined oil obtained by the first hydrogenation refining and the mixed oil is used as a gas turbine fuel oil.

Description

FUEL-OIL (FUEL) FOR GAS TURBINE, METHOD OF PRODUCTION OF THE GAS AND METHOD FOR THE GENERATION OF ENERGY TECHNICAL FIELD This invention relates to the fuel oil for a gas turbine, and more particularly to the fuel oil for the gas turbine used for the generation of energy by the gas turbine, to a method for producing fuel oil for the gas turbine. gas and a method for generating energy using fuel oil for the gas turbine.

BACKGROUND OF THE INVENTION In general, the thermal energy generation of the oil is adapted to generate steam at a high pressure in a boiler using a crude oil and / or heavy oil as a fuel for the boiler, to rotate by means of this a gas turbine by means of the steam thus generated, leading to the generation of energy. However, such a system is of reduced efficiency in power generation. Commonly, a large-sized, high-efficiency oil-burning boiler has already been developed, however, it only exhibits a REF: 128914 generation efficiency as low as approximately 40%. Thus, this causes a large part of the energy to be discharged to the outside in the form of a greenhouse gas without being recovered. In addition, this causes a certain amount of SOx to be present in the exhaust gas or combustion gas to be discharged therefrom. Although the exhaust gas is subjected to the desulfurization of the combustion gas, the SOx is partially discharged to an ambient atmosphere, leading to environmental contamination. In addition, a system for generating the combined cycle power of the gas turbine is executed, which is adapted to drive a gas turbine for the generation of energy using natural gas as a source of heat for it and recover the heat Disposal of combustion gas or high temperature exhaust gas discharged from the gas turbine for the production of steam, to thereby drive a steam turbine, leading to the generation of energy. The system has come to be appreciated in the art because it has an increased efficiency in power generation, a reduction in the amount of C02 generated per unit of power generation and a high reduction in SOx content. and NOx in the combustion gas. When natural gas is used as the feed gas, it is required to transport it from a gas field to a power generation plant through a storage pipeline or LNG and gasify it, followed by gas combustion in the gas turbine . Unfortunately, this leads to an increase in the cost of the equipment. In view of the foregoing, a method for producing fuel oil for a gas turbine is proposed as described in the Published Publications of Japanese Patent Applications Nos. 207179/1994 and 209600/1994. The techniques described in the first Japanese publication are interpreted to subject a crude oil of low sulfur content having a salt content adjusted to be 0.5 ppm or less to a separation treatment by atmospheric distillation or vacuum distillation to produce the fuel oil of the gas turbine constituted of a low boiling fraction of 0.05% by weight in the sulfur content. The techniques described in this latest Japanese Publication are adapted to heat crude oil with low sulfur content using waste heat discharged from a gas turbine and then acting on hydrogen on low sulfur crude oil, to reduce by half of this the content of sulfur and heavy metals in crude oil, followed by the recovery of crude oil thus refined, which is then used as fuel oil for the gas turbine. Now, an environmental problem has come to be appreciated in art. Therefore, it is required to greatly minimize the content of a sulfur compound in the combustion gas. This could be solved by the use of a desulphurization unit of the combustion gas. Unfortunately, in the generation of energy using the gas turbine fuel oil, the arrangement of the desulphurisation unit of the combustion gas causes the deterioration in the efficiency of the generation of energy due to a loss of pressure, so that it is required to minimize a sulfur content of the fuel oil of the gas turbine. Thus, the techniques of the first Japanese publication cause that the amount of oil burning is considerably restricted in atmospheric distillation or vacuum distillation, in order not to increase by this the amount of light oil or light distillate that is going to be fed to the gas turbine or the amount of fuel oil from the gas turbine. This causes the gas turbine fuel oil yields based on crude oil to be as low as a 40% level, even if the Middle East (Middle East) crude oil which has a low sulfur content is used. An increase in the burning of oil with the purpose of increasing yields causes an increase in sulfur production. Also, when they are applied to crude oil which is readily available and has an increased sulfur content, recovery of light oil or light residue in the same amount causes a sulfur content of the light oil to exceed a specified level, so that it is unsuitable for use as a fuel oil for a gas turbine. Thus, there is a requirement to reduce the recovery of light oil, leading to the application of crude oil that is technically and economically disadvantageous. The latest Japanese publication describes techniques for producing hydrogen using methanol as a starting material and subjecting crude oil to hydrotreatment with the hydrogen thus produced. However, there are technical proposals to treat crude oil at a low sulfur content, so that the application of the techniques to crude oil with a high sulfur content are considerably restricted. In addition, hydrotreating is carried out on the crude oil instead of on the light oil or the light distillate obtained by the distillation of the crude oil, so that it is required to accommodate the process conditions to the heavy oil or the residue contained in the oil. Raw oil. This requires increasing a reaction temperature, a reaction pressure and the reaction time or a period of time during which the heavy oil is kept in contact with a catalyst in the reaction. Unfortunately, this causes the excessive fractionation of the light oil in the crude oil, leading to the LPG or similar that is contained in a large quantity in the fuel oil for a gas turbine, so that the storage of the fuel oil causes a part of it is gasified. This requires increasing the pressure resistance of a tank to a significantly high level. Also, the temperature of the reaction and the reaction pressure are caused to increase, so that a reaction vessel for hydrotreating is complicated in its structure and has an increased manufacturing cost. In addition, an increase in reaction time requires a large dimensioning of a catalyst carrier, leading to a large dimensioning of the reaction vessel and an increase in the consumption of a catalyst.

DESCRIPTION OF THE INVENTION The present invention has been made in view of the preceding disadvantage of the prior art.

Accordingly, it is an object of the present invention to provide a method for producing a gas turbine fuel oil which is capable of producing the gas turbine fuel oil from the feedstock, with increased efficiency . It is another object of the present invention to provide a method of generating energy that uses the fuel oil of the gas turbine thus produced. In accordance with one aspect of the present invention, a method for producing the gas turbine fuel oil from the feed oil with increasing yields is provided. The method includes an atmospheric distillation step of subjecting the crude oil that acts as the feed oil to an atmospheric distillation to separate the crude oil in light oil and atmospheric residual oil, a first step of hydrotreating to put in contact the light oil produced in the atmospheric distillation step with the hydrogen pressurized in the presence of a catalyst in the form of clods, to carry out by means of this a removal treatment of the impurities, leading to the obtaining of the refined oil, and a first step separation, the separation of atmospheric residual oil into a light oil material and a heavy oil material. The first separation step is selected from the group consisting of vacuum distillation, solvent deasphalization, thermal fractionation and steam distillation. The method also includes a second hydrotreating step for contacting the light oil material produced in the first step of the separation with the pressurized hydrogen in the presence of a catalyst, to thereby carry out a removal treatment of the impurities, leading to obtaining a refined oil. The fuel oil of the gas turbine obtained in the first and second hydrotreating steps is 4 cSt or less in its viscosity at 100 ° C, contains alkali metals in an amount of 1 ppm or less, lead (Pb) in a amount of 1 ppm or less, V in an amount of 0.5 ppm or less, Ca in an amount of 2 ppm or less and sulfur in an amount of 500 ppm or less, and is produced with yields of 65% or more based on the food oil. In a preferred embodiment of the present invention, the method also includes a second separation step for separating the heavy oil material produced in the first separation step in the light oil material and a heavy oil material. The second separation step is selected from the group consisting of deasphalting with solvents and thermal fractionation. The method further includes a third step of hydrotreating or refining the light oil material produced in the second separation step, to thereby obtain the refined oil, which is used as the fuel oil of the gas turbine. In a preferred embodiment of the present invention, at least two of the first, second and third hydrotreating steps are executed as a common step. Thus, in the present invention, the first hydrotreating is carried out subsequent to the atmospheric distillation, so that the atmospheric distillation can be carried out although there is no news of the amount of the sulfur and the metals that are introduced to the material of light oil. Also, by practicing the second step of hydrotreating after the first step of separation, conditions are allowed for the first step of the separation to be determined to increase the amount of light oil material produced, without taking into account sulfur and metals, of so that the fuel oil of the gas turbine can be produced with increased yields based on the feed oil. The present invention is directed to the fuel oil of the gas turbine; consequently, the first hydrotreating is performed only by subjecting a plurality of light oil fractions produced in the atmospheric distillation column to hydrotreatment in one assembly, leading to a reduced equipment cost. The fuel oil of the gas turbine of 4 cSt viscosity at 100 ° C exhibits satisfactory combustion properties. Also, the metal and the sulfur contained in the fuel oil of the gas turbine are in a trace quantity, so that the combustion of the fuel oil can be carried out at a temperature as high as approximately 1300 ° C. In a preferred embodiment of the present invention, the method further includes a fourth hydrotreating step of contacting the heavy oil material produced in the first separation step with the pressurized hydrogen in the presence of a catalyst, to be carried out by means of this a treatment of removal of the impurities and the fractionation of a part of the heavy oil material, leading to the obtaining of a refined oil and a heavy oil material. The refined oil produced in the fourth step of hydrotreating is used as the fuel oil of the gas turbine. The first separation step can be replaced with a hydrotreating step (fifth step of hydrotreating). In this case, the method may further include a third separation step for separating the heavy oil material produced in the fifth separation step into a light oil material and a heavy oil material. The third separation step is selected from the group consisting of vacuum distillation, deasphalting with solvents and thermal fractionation. The light oil material produced in the third separation step is used as the fuel oil of the gas turbine. In a preferred embodiment of the present invention, the fuel oil of the gas turbine is further subjected to atmospheric distillation, to thereby provide the fuel oil of the light gas turbine and the fuel oil of the turbine. of gas heavier than the fuel oil of the gas turbine, light. The heavy oil material produced in the last separation step or the heavy oil material produced in the fourth hydrotreating step can be used as the fuel oil for a boiler. In the present invention, a material for hydrogen is not limited to any specific. In a preferred embodiment of the present invention, the heavy oil material obtained from the feed oil can be partially oxidized by oxygen to produce hydrogen, which can be used in the hydrotreating steps. The heavy oil material which is produced in the first separation step can be used for this purpose.

Also, in accordance with this aspect of the present invention, a method for producing the fuel turbine of the gas turbine from the feed oil with increased yields is provided. The method includes a first separation step for the separation of the heavy feed oil consisting of the atmospheric residual oil obtained by the atmospheric distillation of the crude oil and / or the heavy oil in a light oil material and a heavy oil material. The first separation step can be selected from the group consisting of vacuum distillation, deasphalting with solvents, thermal fractionation and steam distillation. Also, the method includes a second hydrotreating step of contacting the light oil material produced in the first separation step with the pressurized hydrogen in the presence of a catalyst, to thereby carry out a removal treatment of impurities, leading to obtaining refined oil. The fuel oil of the gas turbine which is the refined oil thus obtained, is 4 cSt or less of viscosity at 100 ° C, contains the alkali metal in an amount of 1 ppm or less, lead in an amount of 1 ppm or less, V in an amount of 0.5 ppm or less, Ca in an amount of 2 ppm or less and sulfur in an amount of 500 ppm or less, and is produced in yields of 40% or more based on the heavy oil of feeding. In a preferred embodiment of the present invention, the method may further include a second separation step for separating the heavy oil material produced in the first separation step into a light oil material and a heavy oil material. The second separation step is selected from the group consisting of solvent deasphalting and thermal fractionation. The method further includes a third hydrotreating step of refining the light oil material produced in the second separation step, whereby the refined oil is obtained, which is used as the fuel oil of the gas turbine. In a preferred embodiment of the present invention, the method may include a fourth hydrotreating step for contacting the heavy oil material produced in the first separation step with the pressurized hydrogen in the presence of a catalyst, to be carried out by means of this a treatment of removal of the impurities and the fractionation of a part of the heavy oil material, leading to the obtaining of the refined oil and a heavy oil material, in which the refined oil produced in the fourth step of hydrotreating is used as the fuel oil of the gas turbine.

Further, in accordance with this aspect of the present invention, a method of producing the gas turbine fuel oil from the feed oil with increased yields is provided. The method includes a fifth hydrotreating step for contacting the heavy oil in the feed consisting of the atmospheric residual oil obtained by the atmospheric distillation of the crude oil and / or the heavy oil with the pressurized hydrogen in the presence of a catalyst, for carry out a treatment of removal of impurities and fractionation as a part of a heavy oil material, leading to obtaining a refined oil and a heavy oil material. The gas turbine fuel oil which is the refined oil thus obtained in the fifth hydrotreating step is 4 cSt or less in viscosity at 100 ° C, contains alkali metals in an amount of 1 ppm or less, lead in an amount of 1 ppm or less, V in an amount of 0.5 ppm or less, Ca in an amount of 2 ppm or less and sulfur in an amount of 500 ppm or less, and is produced with yields of 40% or more with base in the heavy oil feed. In this case, the method may further include a third separation step to separate the heavy oil material produced in the fifth step of hydrotreating, in a light oil material and a heavy oil material. The third separation step is selected from the group consisting of vacuum distillation, deasphalting with solvents and thermal fractionation. The light oil material produced in the third separation step is used as the fuel oil of the turbine. Accordingly, in the present invention, the crude oil is subjected to atmospheric distillation, whereby it can be separated into light oil or light distillate and atmospheric residual oil. The light oil is then hydrotreated and the residual atmospheric oil is subjected to the hydrotreatment separation treatment, leading to a light oil material being produced. The light oil material thus obtained is then subjected to hydrotreating, to thereby provide the refined oil, which is used as the fuel oil of the gas turbine. Accordingly, the present invention allows the fuel oil of the gas turbine to be produced in increased yields while ensuring a high quality of the fuel oil. According to another object of the present invention, the fuel oil of the gas turbine is provided, which is produced according to the method described above. In addition, according to a further aspect of the present invention, a method of generating energy is provided. The energy generation method includes the steps of operating a gas turbine using the gas turbine fuel oil produced as described above as the fuel to carry out the generation of the energy and use the exhaust gas of the gas turbine. high temperature discharged from the gas turbine as a heat source for a waste heat recovery boiler and driving or driving a gas turbine by means of the steam generated in the waste heat recovery boiler, leading to achieving the generation of energy.

BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a schematic block diagram showing a system for executing a method for producing a fuel oil of the gas turbine according to the present invention by way of example; Figure 2 is a schematic view showing another example of removal of light oil or light distillate from an atmospheric distillation column in the system shown in Figure 1; Figure 3 is a schematic block diagram showing a hydrotreating unit by way of example; Figure 4 is a schematic view showing an essential part of a hydrogen plant in the manner of example; Figure 5 is a schematic block diagram showing another example of a system for practicing a method according to the present invention; Figure 6 is a schematic block diagram showing a further example of a system for practicing a method according to the present invention; Figure 7 is a schematic block diagram showing yet another example of a system for practicing a method according to the present invention; Figure 8 is a schematic block diagram showing yet another example of a system for practicing a method according to the present invention; Figure 9 is a schematic block diagram showing yet another example of a system for practicing a method according to the present invention; Figure 10 is a schematic block diagram showing a still further example of a system for practicing a method according to the present invention; Figure 11 is a schematic block diagram showing a still further example of a system for practicing a method according to the present invention, Figure 12 is a schematic view showing a partial oxidation unit incorporated in the system shown in Figure 10 by way of example; and Figure 13 is a diagrammatic view showing the manner of using the fuel oil of the gas turbine produced by the present invention by way of example.

BEST MODE FOR CARRYING OUT THE INVENTION Referring first to Figure 1, a system suitable for practicing a method for producing the fuel oil of the gas turbine according to the present invention is illustrated by way of example. In each of the embodiments described hereinafter, hydrotreating is executed. In the following description, the first to fifth steps of hydrotreating will be carried out depending on the hydrotreating stages. The gas turbine fuel oils obtained in the hydrotreating steps are generally used as they are mixed together. Thus, the following modalities will be described in relation to the fuel oil of the mixed gas turbine. However, the present invention can be practiced without mixing the fuel oils, wherein the fuel oils are used separately from each other.

The feed oil 1 may be constituted by crude oil. The feed oil 1 is first subjected to a desalting treatment in a deasphalting section 11 under conditions such as those conventionally employed in the oil refinery. The treatment is carried out in such a way that the feed oil and the water are mixed together, to transfer the salt by means of this and a muddy matter to an aqueous phase, leading to an alkali metal which adversely affects a gas turbine is removed. The feed oil thus desalted is then fed to an atmospheric distillation column 2, leading to it being separated, for example, in the light oil or the light distillate 21 having a boiling point below 340 to 370 ° C and the residual oil (atmospheric residual oil) 22 higher than 340 to 370 ° C at the boiling point. The light oil 21 thus separated is then fed to a first hydrotreating unit 3. A conventional atmospheric distillation column 2 of an oil refinery is generally constructed in such a way that a plurality of intake openings of the fraction are arranged to be distributed in order from a top of the atmospheric distillation column to a bottom thereof in a manner that corresponds positionally to the boiling points of the fractions such as kerosene, gasoline and the like, because light oil or light distillate contains fractions that range from a high boiling point to a lower boiling point. This leads to the fractions of the light oil that are taken from the intake openings when desired, respectively. In contrast, the illustrated embodiment is constructed to allow the light oil or light distillate 21 to be taken in a clustered form, for example, from an upper part of the atmospheric distillation column 2 while maintaining the oil fractions. lightly blended together, followed by feeding the light oil to the hydrotreating unit 3. Alternatively, the embodiment illustrated, as shown in Figure 2, can be constructed so that the fractions within the regions of the points of The respective boiling points are taken from a plurality of intake openings of the atmospheric distillation column 2 as in the prior art, respectively. Then, the fractions are mixed together, followed by feeding them to the hydrotreating unit 3, where the fractions are subjected concurrently to the hydrotreatment. In Figure 2, the atmospheric distillation column 2 is provided with four such intake openings. More specifically, the production of the fuel oil for automobile with counterflow or batch desulfurization, generally causes operating conditions such as a temperature, a pressure, a catalyst and the like, to be varied, because gasoline, kerosene and heavy oil are different in the level of desulphurisation from each other. On the other hand, in the production of the fuel oil of the gas turbine carried out by subjecting the light oil or the light distillate having a boiling point, for example, below 350 ° C, to countercurrent desulfurization, only it requires to conform the operating conditions to the specifications of the fuel oil of the gas turbine as a whole, thus, the operating conditions are considerably different from those in a refinery. This allows the light oil or light distillate produced in the atmospheric distillation column 2 to be concurrently subjected to hydrotreatment in a common unit, as described above. The atmospheric distillation process produces light oil and a light distillate which contains a plurality of different fractions at their boiling point. The illustrated embodiment is directed to a fuel oil of the gas turbine, so that the fractions of the light oil can be treated in the hydrotreating unit or as a whole. Such concurrent treatment allows a cost of equipment that is to be minimized. The hydrotreating techniques which can be applied to a system of the embodiment illustrated allow the operation at a high temperature, because the shape of the fuel oil of the gas turbine is out of question unlike the hydrotreating step carried carried out in a refinery for the production of the fuel oil for the automobile where the operation is carried out at a low temperature and at a high pressure to avoid the coloring of the fuel oil of the automobile during hydrotreating. This allows a reactor to be of reduced cost because it is operated at a low pressure, leading to a further reduction in the cost of the equipment. Now, the hydrotreating unit 3 and the hydrotreating carried out therein will be described with reference to Figure 3. The light oil or the light distillate 21 is mixed with the pressurized hydrogen gas and then fed through the top of a reaction column 31 therein. The reaction column 31 is provided therein with a catalyst layer 32, which includes a carrier and a catalyst carried on the carrier. This leads to the light oil and light distillate 21 and hydrogen gas passing through the catalyst layer 32 and then being fed from a lower part of the reaction column 31 through a pipe 33 for feeding from the liquid to an elevated pressure tank 34. A slight amount of heavy metals such as vanadium, nickel, lead and the like, which are included in the light oil 21 or continue to be introduced to the hydrocarbon molecules, as well as sulfur and nitrogen, are reacted with hydrogen during a period of time in which the they pass through the catalyst layer 32, whereby they can be detached or removed from the hydrocarbon molecules. This leads to the heavy metals being adsorbed on a catalyst surface and the sulfur and nitrogen being reacted with the hydrogen to form the hydrogen sulphide and the ammonia, respectively. The alkali metals which are dissolved in water slightly, contained in a petroleum material or present in the form of salts, are adsorbed on the surface of the catalyst. The metals are usually contained in the heavy oil or residue, leading to them being present in a trace amount in the light oil 21. From the bottom of the reaction column 31 is discharged the mixed fluid from the oil and the pressure gas elevated at a pressure as high as 30 to 80 kg / cm2, which is then fed to the high pressure tank 34, where the hydrogen gas is separated from the mixture. The hydrogen gas is increased in pressure by means of a CP compressor and then fed circulatoryly into the reaction column 31. A liquid material separated from the hydrogen in the high pressure tank 34 is fed through the pressure regulator pV to a low pressure tank 35, leading to it being reduced in pressure, for example, in approximately 10 to 30%. This leads to a liquefied gas such as hydrogen sulfide, ammonia and the like, dissolved in the liquid material or oil that is vaporized. The refined oil, which is the liquid thus separated, constitutes the fuel oil of the gas turbine. The reference character 35a designates a pump. The gas separated in the low pressure tank contains unreacted hydrogen gas and hydrogen compounds such as hydrogen sulfide, ammonia and the like, as well as the methane produced by cutting off a portion of the hydrocarbon molecules and a hydrocarbon material. light oil that extends from a fraction of liquefied petroleum gas to light naphtha. The term "light oil material" used herein, indicates an ingredient lighter than light oil or light distillate 21. The gas separated in tank 35 is fed to a removal section of impurities 36, where the sulfide Hydrogen and ammonia contained in the gas are removed from it. The impurity removal section 36 can be provided therewith with a liquid absorption layer to absorb impurities such as, for example, hydrogen sulfide and ammonia, so that the passage of the gas through the layer of the absorption liquid allow the impurities to be removed from the gas. The gas from which the impurities are thus removed contains a mixed gas 42 of unreacted hydrogen gas and a light oil material reduced in the number of carbon atoms such as methane and the like. The mixed gas 42 is fed to a hydrogen plant 4, wherein the light oil material in the mixed gas 42 is used as a material for the production of the hydrogen gas. A part of the light oil 21 separated in the atmospheric distillation column 2 is also fed to the hydrogen plant 4, to be used by it as a material for the production of the hydrogen gas. When the feed oil for the production of the hydrogen gas is limited to the heavy oil, the naphtha can be introduced externally to the hydrogen plant 4 only at the start time of the plant 4. The hydrogen gas fed to the column of the reaction 31, as described above, is used circulatoryly, during which the hydrogen gas contained in the gas in a circulation route 37 is incrementally increased, while a light oil material such as methane and the like is gradually increased. This leads to hydrogen gas which is relatively reduced. To avoid such a situation, hydrogen gas 41 is supplied from the hydrogen plant 4 to the circulation path 37, whereby hydrotreating is ensured. The hydrogen plant 4 can be constructed in such a manner as shown in Figure 4. The hydrogen plant 4 includes a combustion furnace 43 in which the fuel gas is burned, as well as the reaction pipes 44 distributed in the furnace. 44. A light oil material such as methane and steam is introduced into the reaction pipes 44, so that the petroleum material or light oil is subjected to steam reforming, whereby the production of hydrogen and the underproduction of carbon monoxide. Then, the carbon monoxide and a light oil material that did not react are modified or removed from the gas, to thereby obtain the hydrogen gas. The removal or refining treatment can be carried out, for example, by oscillating pressure adsorption (PSA), oscillating temperature adsorption (TSA), low temperature separation, film separation or the like. The first to fifth hydrogenation steps in the present invention can each contact the light oil or light oil material with the hydrogen under pressure in the presence of a catalyst, to carry out by this any of (1) ) hydrodesulphurisation or hydrotreating for desulfurization, for the removal of impurities such as a sulfur compound and the like, (2) hydrorefining for an improvement in the properties of light oil or light oil material due to saturation of the unsaturated or similar hydrocarbons and (3) hydrofractionation for the transformation of the oil or the oil material into a lighter oil material. A main object of the first hydrotreating step is to achieve the desulfurization (1) described above, and that each of the second and third hydrotreating steps are to effect the desulfurization (1) and the hydrofineration (2) described above, and that each one of the fourth and fifth steps of hydrotreating are to carry out the desulphurisation (1), the hydrofineration (2) and the hydrofraction (3) described above.

Now, a process carried out in the first hydrotreating unit 3 will be described. The refining of conventional oil is applied separately to naphtha, kerosene, heavy oil and the like contained in light oil or light distillate and subject each of the fractions from a narrow boiling range to hydrotreating. In contrast, the present invention subjects all fractions distilled by atmospheric distillation to hydrotreatment concurrently or in a pooled manner. Thus, the present invention allows the amount of the hydrotreated material to be substantially increased when compared to the prior art. The hydrotreating conditions such as the pressure of the hydrogen gas, a reaction temperature and the like can be varied depending on the type of the oil to be hydrotreated, an object of the hydrotreating and the like. More specifically, the temperature and pressure of the hydrogen gas can be selected within a range of 330 to 380 ° C and a range of 20 to 80 kg / cm2, respectively. In particular, the pressure of the hydrogen gas is preferably set to be within a range of 30 to 70 kg / cm2. Also, the catalyst can be selected from those for hydrotreating in the conventional manner known in the art. The catalyst is preferably formed by carrying the sulfide of Ni, Mo or Co on alumina. When the light Arabian oil is going to be treated, the pressure of the hydrogen gas can be set within a range of 30 kg / cm2 and 50 kg / cm2, leading to the fuel oil of the gas turbine that is provided, which has a sulfur concentration of 450 ppm or less and a nitrogen concentration of 30 ppm or less. In this case, an increase in the hydrogen gas pressure of 40 to 70 kg / cm2 allows an increase in the collision energy of the hydrogen against the molecules of the petroleum ingredient, so that the concentration of the sulfur and the concentration of the nitrogen can be reduced to 200 ppm or less and 20 ppm or less, respectively. The residual oil (residual atmospheric oil) 22 separated in the atmospheric distillation column 2 is fed to a vacuum distillation column 5, wherein the residual oil is separated into a light oil material (light oil material under vacuum). 565 ° C at the atmospheric boiling point which is the lightest fraction in the residual oil 22 and a heavy oil or residue material (vacuum residual oil) 52 having an atmospheric boiling point above 565 ° C. The light oil material 51 is fed to a second hydrotreating unit 6, so that it is subjected to hydrotreatment by this.

The hydrogen gas used in the second hydrotreatment is fed from the hydrogen plant 4 described above thereto. The gas reduced in the number of carbon atoms such as methane or the like, which is produced in the second hydrotreating unit 6 is fed in the form of a feed material to the hydrogen plant 4. When the light oil Arab described above is used as the feed oil, setting a hydrogen gas pressure in the range of 30 to 60 kg / cm2 in the second hydrotreating unit 6 allows the sulfur concentration and nitrogen concentration to be as low as 2000 ppm or less and 2000 ppm or less, respectively. Also, a hydrogen gas pressure of 50 to 100 kg / cm2 reduces the concentration of the sulfur and the concentration of the nitrogen to a level of 1000 ppm or less and to that of 100 ppm or less, respectively. The light oil material thus produced in the second hydrotreating unit 6 is mixed with the light oil material (fuel oil of the gas turbine) produced in the first hydrotreating unit 3 (mixing step), to be used by it as the fuel oil of the gas turbine. The heavy oil material (vacuum residual oil) 52 separated in the vacuum distillation column 5 is separated into a light oil or deasphalted oil material 72 and a heavy oil or deasphalted waste oil material 73 in a deasphalting unit with solvents or solvent extraction unit 71. The separation is carried out by feeding the vacuum residual oil 52 and a solvent from an upper part of the column and a lower part thereof to unit 71 to subject both to a counterflow contact, respectively, leading to the light and heavy oil materials in the vacuum residual oil material 52 which are separated from each other due to a difference in the solubility of the solvent. The deasphalted oil 72 thus separated is mixed with the light oil material 51 from the vacuum distillation column 5 and then fed to the second hydrotreating unit 6. The deasphalted residual oil 73 is subjected to the adjustment of the viscosity when required and then used as the heavy feed oil or the fuel oil for a boiler. Thus, the hydrotreatment carried out in the first hydrotreating unit 3 and that in the second hydrotreating unit 6 corresponds to the first hydrotreating step and the second hydrotreating step, respectively, and the vacuum distillation carried out in the hydrotreating column. vacuum distillation 5 and treatment in the deasphalting unit with solvents 71 corresponds to the first and second separation steps, respectively. The illustrated embodiment allows the gas turbine fuel oil which meets the requirements of the constitution defined in the "DESCRIPTION OF THE INVENTION" to be provided herein. In the illustrated embodiment, the atmospheric distillation step and the vacuum distillation step each are followed by the hydrotreating step, so that each of the distillation steps can be carried out ignoring the amount of the sulfur and heavy metal, leading to an increase in the amount of light oil material. Therefore, when crude oil is used as the feed oil, the gas turbine fuel oil can be produced with yields as high as 65% or more and preferably 70 to 90% (weight ratio) based on the crude oil. Also, when heavy feed oil consisting of atmospheric distillation residue and / or heavy oil, is the starting feed oil, the gas turbine fuel oil can be produced with yields as high as 40% or more and preferably 40 to 75% (weight ratio) based on the heavy feed oil. More specifically, assuming that the crude oil is fed in a relative amount of 100 to the atmospheric distillation column 2, the light oil and the atmospheric residue are distilled at a ratio of 60:40 therein. A light oil material and the vacuum residue can be distilled at a ratio of 40:20 based on the atmospheric residue in a relative amount of 40. In addition, the residual oil under vacuum in a relative amount of 20 can be treated in the unit of deasphalting with solvents 71, leading to a deasphalted oil and a deasphalted residue that is produced at a relative proportion of 10:10. When crude oil is used as the starting feed oil, the gas turbine fuel oil can be produced, which contains a light oil material, a light vacuum oil material and deasphalted oil at a ratio or relative proportion of 60:20:10, leading to yields that are 90%. The yields are as high as 80% even when the deasphalting treatment is executed. Accordingly, the present invention, when crude oil is used as the starting feed oil, provides the gas turbine fuel oil at yields of 65% or more and preferably 70 or 90% depending on the type of oil of food. In addition, the heavy-feed oil consisting of atmospheric residual oil and / or heavy oil is used in a relative amount of 100 as the starting feed oil, a light oil material and a vacuum residue can be distilled to a relative ratio of 50:50 in the vacuum distillation column 5. The residue under vacuum in a relative amount of 50 allows the deasphalted oil and deasphalted residual oil to be produced at a relative ratio of 25:25 in the deasphalting unit with solvents 71. Accordingly, when the heavy oil is used as the starting oil, the gas turbine fuel oil consisting of a light vacuum oil material and the deasphalted oil with solvents in a relative amount of 50:25 can be obtained, leading to yields that are 75%. Yields are maintained at a level as high as 50% even when deasphalting treatment is not carried out. In Figure 1, the dotted lines indicate that the heavy oil is subjected to the deasphalting treatment and then fed to the vacuum distillation column 5. The present invention, when the heavy feed oil described above is used as the starting oil in view of a variation due to the difference in the type of feed oil, it allows the fuel oil of the gas turbine to be produced with yields of 40% or more preferably from 40 to 75%. The present invention is proposed to carry out the hydrotreating on the light oil or the light distillate after the distillation step instead of the direct hydrotreating of the crude oil, so that it is only required to determine the conditions of the reaction in accordance with the oil light. Thus, an increase in the pressure and the temperature of the reaction can be minimized and the reaction time can be reduced, leading to the simplification of the system. Also, the present invention is directed to the fuel oil of the gas turbine, leading to the fractions produced in the distillation step which are hydrotreated concurrently or in a grouped form, leading to the simplification of the process. In the present invention, the heavy oil can be fed to the vacuum distillation column 5 as indicated in the dotted lines in Figure 1. Alternatively, the heavy oil can be fed to the deasphalting unit with solvents 71. Such a feed it does not affect a series of steps started feeding the crude oil to the atmospheric distillation column 2. Therefore, this does not affect the gas turbine fuel oil yields produced from crude oil. The fuel oil of the gas turbine is increased simply by an increase in the additional feed oil, thus, it is within the scope of the present invention. Furthermore, the present invention is not limited to the construction that the light oil material produced in the second separation step or the deasphalted oil 72 produced in the solvent deasphalting unit 71 be treated in the second hydrotreatment unit 6. consequently, it may be treated in a third hydrotreating step or a third hydrotreating unit 60 separately distributed from the second hydrotreating unit 6. The common practice of the second and third hydrotreating steps as in the embodiment shown in Figure 1 it requires determining the conditions of the reaction in accordance with the heavy oil material, leading to a pressure of the hydrogen gas which is at a level as high as, for example, 50 to 150 kg / cm2. On the contrary, the practice of the steps in a manner that are separated from each other, leads to the pressure of the hydrogen gas in the second and third steps being 50 to 150 kg / cm2 and 80 to 200 kg / cm2, respectively. Thus, the separate practice allows the amount of the material treated in the third hydrotreating step to be significantly reduced, so that a pressure-resistant reaction vessel can be reduced in size. In any case, the system can be advantageously constructed depending on the scale thereof and the like, as desired. In the present invention, in the practice of the first to third hydrotreating steps, the first and third steps may be carried out in a common or concurrent manner. Alternatively, the first to third steps can be carried out commonly. In the present invention, the first separation step for subjecting the residual oil 22 produced in the atmospheric distillation unit 2 to the separation treatment is not limited to vacuum distillation. It can be executed by steam distillation, deasphalting with solvents, thermal fractionation by heating the residual oil 22 at a temperature, for example, from 430 to 490 ° C to cut the hydrocarbon molecules by means of energy. thermal, to produce by this a light oil material and a heavy oil material, or the like. The execution of the first separation step by deasphalting with solvents can be carried out in a manner such as that shown in Figure 6, which illustrates another embodiment of the present invention. The atmospheric residual oil 22 is fed to a solvent deasphalting unit 81, leading to it being separated into a light oil material (deasphalted oil with solvents) 82 and a heavy oil material (residual oil deasphalted with solvents) 83. Light oil material 82 is fed to the second hydrotreating unit 6. In the embodiment shown in Figure 6, a second separation step is not carried out. However, the residual oil deasphalted with solvents 83 can be subjected to the second separation step as in the embodiment shown in Figure 1. The second separation step can be practiced by such thermal fractionation as described above. The heavy oil material separated in the first separation step can be subjected to hydrotreating as shown in Figure 7, which shows a further embodiment of the present invention. More particularly, a heavy oil material (deasphalted waste oil) 83 separated in a solvent deasphalting unit 81 is fed to a fourth hydrotreatment unit 91, whereby it can be separated into a light oil material 92 and a material of heavy oil 93. The fourth hydrotreatment unit 91 is placed in a rear stage of the unit shown in Figure 3 and includes a distillation unit for separating the heavy oil material 83 in the light oil material 92 and the oil material. heavy 93 such as, for example, an atmospheric distillation unit or a vacuum distillation unit. The modalities thus constructed also allow each one that the fuel oil of the gas turbine to be obtained from the heavy oil material separated in the first separation step (for example, the step of dealphalting with solvents), leads to the recovery of the fuel oil from the gas turbine will be significantly increased. Alternatively, a portion of the feed oil can be fed to the fourth hydrotreating unit 91 while it is mixed with the heavy oil material 83 separated in the solvent deasphalting unit 81. Also, the present invention can be constructed from such as one shown in Figure 8, which still illustrates another embodiment of the present invention. In the illustrated embodiment, the residual oil 22 separated in an atmospheric distillation step is fed to a fifth hydrotreating unit 101, wherein a fifth hydrotreating step is carried out to separate the residue 22 in a light oil material 102 and a heavy oil material 103, so that the light oil material 102 can be mixed with the gas turbine fuel oil produced in a first hydrotreating unit 3. The fifth hydrotreatment unit 101 includes a distillation unit as in the fourth hydrotreatment unit 91. The heavy oil material 103 is fed to a solvent deasphalting unit 111, so that it is separated by it in a light oil material (deasphalted oil) 112 and a heavy oil material (oil residual deasphalted) 113. The light oil material 112 thus separated is used as the fuel oil of the gas turbine while it is mixed with, for example, the light oil material 102 produced in the fifth hydrotreating unit 101, and the heavy oil material 113 is used as, for example, the fuel oil for a boiler. A third separation step is not limited to a step of deasphalting with solvents and can be executed in the form of a thermal fractionation step or a vacuum distillation step. The illustrated embodiment similarly allows the recovery of the fuel from the gas turbine from the feed oil to be as high as 65% or more and preferably from 70 to 90%. The light oil (gas) material such as methane or the like, produced in each of the fourth hydrotreating unit 91 and the fifth hydrotreating unit 101 shown in Figures 7 and 8 is fed to a hydrogen plant 4 for the production of hydrogen gas. In the embodiments described above, the light oil or light distillate 21 produced in the atmospheric distillation column 2 and the light oil material (light vacuum oil material) 51 produced in the vacuum distillation column 5, are treated in the units of. hydrotreatment different from each other, respectively. Alternatively, the present invention may be constructed as shown in Figure 9, which still illustrates another embodiment of the present invention. In the illustrated embodiment, the light oil 21 and the light oil material 51 are mixed together and then subjected to hydrotreating in a hydrotreating unit 6. Such construction corresponds to a combination of the first hydrotreating unit 3 and the second hydrotreating unit. hydrotreatment 6 in the embodiment shown in Figure 1. In general, the reaction conditions for hydrotreating are determined in accordance with a heavy oil material contained in the feed oil. In the illustrated embodiment, the heavy oil material corresponds to the light oil material (light vacuum oil material) 51. Accordingly, the light oil material 21 and the light oil material under vacuum 51 are treated as a whole while reducing a weight ratio (volume ratio) of the light oil material 21 with respect to the vacuum light oil material 51 in the feed oil. Such treatment eliminates the arrangement of a unit for hydrotreating the light oil material, leading to a reduction in manufacturing cost. An increase in the ratio of the light oil material 21 or a reduction in the ratio of the light oil material to the vacuum 51 requires that the reaction conditions be set in accordance with a heavy oil material corresponding to the light oil material under vacuum 51 in a small amount. This makes the design of the reactor difficult or problematic, leading to failure to satisfactorily exhibit an economic advantage. On the contrary, the setting of the reaction conditions in accordance with the vacuum light oil material 51 contributes to a significant improvement in the refining of the light oil material. In the embodiment shown in Figure 9, the first step of the separation is executed in the form of vacuum distillation as an example. However, the first step of separation can be constituted by any other suitable techniques. A light oil material produced by the techniques and light oil 21 can be treated in a hydrotreating unit 61 concurrently or in a grouped manner. When a process in the hydrotreatment unit 61 is carried out using the light Arabian oil, fixing a pressure of hydrogen gas within a range of 30 to 60 kg / cm2 allows the concentrations of sulfur and nitrogen in the fuel oil of the gas turbine are as low as 500 ppm or less and 50 ppm or less, respectively. An increase in the hydrogen gas pressure at a level of 50 to 100 kg / cm2 allows the sulfur and nitrogen concentrations to be further reduced to levels as low as 300 ppm or less and 30 ppm or less, respectively.

The refined oil produced by the concurrent treatment of the light oil material and the light oil 21 in the hydrotreating unit 61 is sufficient for use as a fuel oil of the gas turbine. Alternatively, the refined oil, as shown in Figure 10, is subjected to distillation at a temperature of, for example, 350 ° C in an atmospheric distillation column 62, so that the resulting light oil material can be used as the fuel oil of the gas turbine of an increased quality and the resulting residual oil can be used as the fuel oil of the gas turbine heavier than the light oil material. The present invention can be so constructed that the heavy oil material produced in the first separation step, the second separation step and / or the third separation step is oxidized by oxygen gas to produce hydrogen, which is then used in a hydrotreating unit. The hydrotreating unit may be the one used in any of the first to fourth hydrotreating steps. Figure 11 illustrates a still further embodiment of the present invention which is constructed to perform such hydrotreating. More specifically, the waste oil fed from a solvent deasphalting unit 81 is subjected to partial oxidation to produce hydrogen, which is then fed to a first hydrotreating unit 3 and a second hydrotreatment unit 6. The reference numeral 63 designates an oxygen plant to remove oxygen from the air and 64 is a unit of partial oxidation. A heavy oil material that is to be partially oxidized is not limited to the residual oil produced in the solvent de-asphalting unit.thus, any residual oil produced in a first separation step in a vacuum distillation column 5 or the like may be partially oxidized. Alternatively, a heavy oil material obtained in a second or third separation step can be used for this purpose. The partial oxidation unit 64 can be constructed as shown in Figure 12. In unit 64 of Figure 12, a heavy oil material and high pressure steam are preheated and then injected into a reaction furnace together with oxygen, so that the gas consisting mainly of CO and H2 can be produced by a partial oxidation reaction under the process conditions of, for example, 1200 to 1500 ° C at the temperature and 2 to 85 kg / cm2 in the pressure. Then, the gas is quenched or cooled rapidly in the range of 200 to 260 ° C by means of water in a quenching chamber placed under the furnace of reaction 65. This allows a large part of the unreacted charcoal to be removed and The steam required for the subsequent CO conversion process is introduced into the gas. The gas is then fed to a scrubbing tower 66, where any remaining unreacted carbon can be completely removed from the gas. Then, it is fed to a CO 67 converter, whereby the CO remaining in the gas is converted to C02 through the reaction of the CO with the vapor by means of, for example, a cobalt-molybdenum catalyst. Subsequently, the oxidation gas such as CO 2 and the like is absorbed in an absorption tower 68 of the acid gas, leading to a hydrogen gas of a very high purity being obtained. The fuel oil of the gas turbine thus provided by the present invention can be used for, for example, power generation, as shown in Figure 13. More particularly, the gas turbine fuel oil is burned in a combustion nozzle, leading to a combustion gas being produced, which is then used to drive or drive a gas turbine 201, so that a generator 202 generates electrical energy. The gas turbine 201 discharges the high temperature exhaust gas, which is fed to a waste heat recovery boiler 203, which generates steam using the heat of the exhaust gas. The steam allows the operation of a steam turbine 204, leading to a generator 205 generating electrical energy. Such power generation allows waste heat from the gas turbine fuel oil to be effectively available, leading to an increase in generation efficiency. The examples of the invention are described after this.

Example 1 Light Arabian crude oil (S content: 1.77% by weight) which is more readily available in the art was used as the feed oil, to produce by this the gas turbine fuel oil by means of the system shown in Figure 1. More particularly, the crude oil was separated into light oil or light distillate 21 of 350 ° C or less of boiling point and heavy oil or residue 22 above 350 ° C boiling point and a pressure of the hydrogen gas in the first hydrotreating step was set to be 45 kg / cm2, leading to the production of the fuel from the gas turbine. Also, the vacuum distillation step provided a light oil material 51 of 565 ° C or less of boiling point (the boiling point below an atmospheric pressure) and a heavy oil material 52 having a boiling point above. of 565 ° C per separation. In addition, a pressure of the hydrogen gas in the second hydrotreating step was set to be 55 kg / cm2, to thereby obtain the fuel oil of the gas turbine, which was then mixed with the fuel. Oil from the gas turbine produced in the first step of hydrotreating. Any alkali metal, alkaline earth metal, V and Pb were not detected in the fuel oil of the gas turbine thus obtained, which had a sulfur concentration of 430 ppm and a viscosity of 1.3 cSt at 100 ° C. The gas turbine fuel oil yields based on the feed oil were 84%. It was found that the fuel oil of the gas turbine can be used for a gas turbine from which an inlet temperature of the gas turbine is 1300 ° C. The simulation was carried out assuming that all the energy obtained from crude oil is converted into energy generation (the generation of energy from the gas turbine and the generation of energy from the boiler). The service power of the station in a refinery plant, the efficiency of the generation of the combined cycle gas turbine and the power generation efficiency of the boiler are set to be 4%, 49% and 38% , respectively. Under such conditions, the final energy recovery was calculated while adjusting the feed of the crude oil to the refinery plant to 100 units in terms of a heating value. As a result, it was found that the motive energy of 45.7 units in terms of a heating value can be recovered.

Comparative Example 1 The gas turbine fuel oil was produced according to the procedure described in Publication No. 207179/1994 Publicly Submitted to the Japanese Patent Application. In the Japanese publication, crude oil with a low sulfur content, of which a salt concentration is adjusted to be 0.5 ppm or less, is used as the feed oil to produce the fuel oil from the gas turbine. which has a sulfur concentration of 0.05% by weight or less. Light Arab oil has an increased sulfur content when compared to so-called low sulfur crude oil. Accordingly, the crude oil was treated according to the procedure described in the Japanese publication, leading to petroleum fractions which have a sulfur concentration of 0.05% by weight or less, which are separated by distillation. The gas turbine fuel oil prepared according to the publication had only fractions ranging from a light naphtha fraction to a kerosene fraction which has a boiling point region of up to 245 ° C. Also, any alkali metal, alkaline earth metal, V and Pb were not detected in the fuel oil of the gas turbine. In addition, it had a sulfur concentration of approximately 470 ppm and a viscosity of 0.3 cSt at 100 ° C, leading to an increased quality. Nevertheless, the gas turbine fuel oil yields based on the feed oil were as low as 24%. The simulation was performed under substantially the same conditions as Example 1 described above, except that the service energy of the station was set to be 3%. The recovery of the final power was calculated while adjusting the supply of crude oil to the refinery plant to 100 units in terms of a heating value. As a result, it was found that the recovery of motive energy in terms of a heating value was as low as 39.5 units. Accordingly, the comparative example was highly inferior in the availability of energy with respect to the present invention.

Example 2 Of Middle Eastern crude oil (Middle East), Ornan crude oil is known to have a relatively low sulfur content. Such crude oil from Ornan was used to produce the fuel oil from the gas turbine by means of the system shown in Figure 1. Ornan crude oil has a sulfur concentration of 0.94% by weight, therefore, it corresponds to the crude oil of low sulfur content described in Publication No. 207179/1994 Publicly Submitted to the Japanese Patent Application. In Example 2, the crude oil was subjected to atmospheric distillation, to be separated by this in light oil or light distillate 21 of 350 ° C or lower at its boiling point and heavy oil or residue 22 which It has a boiling point above 350 ° C. Also, a pressure of the hydrogen gas in the first hydrotreating step was set to be 40 kg / cm2, leading to the production of a fuel oil from the gas turbine. Also, the vacuum distillation step provided a light oil material 51 of 565 ° C or less at its boiling point (the boiling point under atmospheric pressure) and a heavy oil material 52 having a boiling point above. of 565 ° C per separation. In addition, a pressure of the hydrogen gas in the second hydrotreating step was set to be 50 kg / cm2, to thereby obtain a fuel oil from the gas turbine, which was then mixed with the fuel. Oil from the gas turbine produced in the first step of hydrotreating. Any alkali metal, alkaline earth metal, V and Pb were not detected in the fuel oil of the gas turbine so mixed, which had a sulfur concentration of 410 ppm and a viscosity of 1.1 cSt at 100 ° C. The gas turbine fuel oil yields based on the feed oil were 85%. It was found that the fuel oil of the gas turbine can be used for a gas turbine from which an inlet temperature of the gas turbine is 1300 ° C. The simulation was carried out assuming that all the energy obtained from crude oil is converted into power generation (gas turbine power generation and boiler power generation). The service power of the station in a refinery plant, the efficiency of the generation of the combined cycle gas turbine and the efficiency of the generation of the boiler energy were set to be 4%, 49% and 38%, respectively. Under such conditions, the recovery of the final energy was calculated while adjusting the supply of crude oil to the refinery plant by 100 units in terms of a heating value.

As a result, it was found that the motive power of 45.8 units in terms of the heating value can be recovered.

Comparative Example 2 The gas turbine fuel oil was produced from the same Ornan crude oil as in Example 2 described above according to a procedure described in Publication No. 207179/1994 Publicly Submitted to the Japanese Patent Application. The production was carried out as in Comparative Example 1 described above. The crude oil was treated according to the procedure described in the Japanese publication, leading to petroleum fractions which have a sulfur concentration of 0.05% by weight or less, which are separated by distillation. The gas turbine fuel oil prepared according to the publication had only the fractions ranging from a light naphtha fraction to a kerosene fraction which had a boiling point region up to 250 ° C. Also, any alkali metal, alkaline earth metal, V and Pb were not detected in the fuel oil of the gas turbine. In addition, it had a sulfur concentration of approximately 490 ppm and a viscosity of 0.45 cSt at 100 ° C. Nevertheless, the gas turbine fuel oil yields based on the feed oil were substantially reduced to a level as low as 35% without taking into account the fact that the feed oil is a crude oil of low sulfur content . The simulation was performed under substantially the same conditions as Example 2, except that the energy of the service station was set to be 3%. The final energy recovery was calculated while adjusting the feed of the crude oil to the refinery plant to 100 units in terms of a heating value. As a result, it was found that the recovery of motive energy in terms of a heating value was as low as 40.7 units. Thus, the comparative example was highly inferior in the availability of energy with respect to the present invention without taking into account the fact that the feed oil used was of a reduced sulfur content. Accordingly, in the present invention, the crude oil is subjected to atmospheric distillation, so that it is separated by means of this in the light oil or the light distillate and the residual atmospheric oil. The light oil is then hydrotreated and the residual atmospheric oil is subjected to separation or hydrotreating treatment, leading to a light oil material being produced. The light oil material thus obtained is then subjected to hydrotreating, to thereby provide the refined oil, which is used as the fuel oil of the gas turbine. Accordingly, the present invention allows the fuel oil of the gas turbine to be produced with increased efficiency while ensuring a high quality of the fuel oil.

INDUSTRIAL APPLICABILITY This invention allows the fuel oil of the gas turbine to be produced from the feed oil in increased yields.

It is noted that in relation to this date, the best method known to the applicant to carry out the aforementioned invention, is that which is clear from the present description of the invention.

Claims (19)

1. CLAIMS Having described the invention as above, the content of the following claims is claimed as property: 1. A method for producing a fuel oil from the gas turbine from a feed oil with increased yields, characterized in that it comprises: atmospheric distillation step to subject the crude oil that acts as the feed oil to the atmospheric distillation to separate the crude oil in light oil and atmospheric residual oil; a first hydrotreating step for contacting the light oil produced in the atmospheric distillation step with the pressurized hydrogen in the presence of a catalyst in a lump form, to thereby carry out a removal treatment of the impurities , leading to obtaining refined oil; a first separation step for separating the residual atmospheric oil into a light oil material and a heavy oil material; the first separation step is selected from the group consisting of vacuum distillation, solvent deasphalting, thermal fractionation and steam distillation; and a second hydrotreating step for contacting the light oil material produced in the first step of the separation with the pressurized hydrogen in the presence of a catalyst, to thereby carry out a removal treatment of the impurities, leading to obtaining a refined oil; a fuel oil of the gas turbine obtained in the first and second treatment steps which is 4 cSt or less of viscosity at 100 CC, which contains an alkali metal in an amount of 1 ppm or less, lead in an amount of 1 ppm or less, V in an amount of 0.5 ppm or less, Ca in an amount of 2 ppm or less, and sulfur in an amount of 500 ppm or less, and which is produced with yields of 65% or more based on oil of food.
2. 2. A method in accordance with the claim 1, characterized in that the first hydrotreating step and the second hydrotreating step are executed as a common step.
3. A method according to claim 1, characterized in that it further comprises a second separation step for separating the heavy oil material produced in the first separation step into a light oil material and a heavy oil material; a second separation step that is selected from the group consisting of deasphalting with solvents and thermal fractionation; and a third hydrotreating step for the refining of the light oil material produced in the second separation step, to thereby obtain the refined oil, which is used as the fuel oil of the gas turbine.
4. 4. A method according to claim 3, characterized in that at least two of said first, second and third hydrotreating steps are executed as a common step.
5. A method according to claim 1 or 2, characterized in that it further comprises a fourth hydrotreating step for contacting the heavy oil material produced in the first separation step with the pressurized hydrogen in the presence of a catalyst, for to carry out by means of this a treatment of removal of the impurities and the fractionation of a part of the heavy oil material, leading to the obtaining of the refined oil and a heavy oil material; The refined oil produced in the fourth step of hydrotreating is used as the fuel oil of the gas turbine.
6. 6. A method for producing fuel oil from the gas turbine from a feed oil with increased yields, characterized in that it comprises: an atmospheric distillation step for subjecting the crude oil acting as the feed oil to an atmospheric distillation for Separate crude oil into light oil and atmospheric residual oil; a first hydrotreating step for contacting the light oil produced in the atmospheric distillation step with the pressurized hydrogen in the presence of a catalyst in the form of clods, in order to carry out by this a treatment for removal of the impurities , leading to obtaining refined oil; a fifth hydrotreating step for contacting the residual atmospheric oil with the pressurized hydrogen in the presence of a catalyst, to thereby carry out a treatment for removal of the impurities and the fractionation of a part of the heavy oil material , leading to obtaining refined oil and a heavy oil material; the gas turbine fuel oil obtained in the first and fifth steps of hydrotreating is 4 cSt or less of viscosity at 100 ° C, which contains an alkali metal in an amount of 1 ppm or less, lead in an amount of 1 ppm or less, V in an amount of 0.5 ppm or less, Ca in an amount of 2 ppm or less and sulfur in an amount of 500 ppm or less, and that is produced with yields of 65% or more based on the food oil.
7. A method according to claim 6, characterized in that it further comprises a third separation step for separating the heavy oil material produced in the fifth separation step into a light oil material and a heavy oil material; The third step of separation is selected from the group consisting of vacuum distillation, deasphalting with solvents and thermal fractionation; The light oil material produced in the third separation step is used as the fuel oil of the gas turbine.
8. 8. A method as defined in any of claims 1 to 7, characterized in that the fuel oil of the gas turbine is further subjected to atmospheric distillation, to provide by this the light fuel oil of the gas turbine. and the heavy fuel oil of the gas turbine, heavier than the light fuel oil of the gas turbine.
9. A method according to any of claims 1 to 4 and 7, characterized in that the heavy oil material produced in the last separation step is used as the fuel oil for a boiler.
10. 10. A method according to claim 5, characterized in that the heavy oil material produced in the fourth hydrotreating step is used as the fuel oil for a boiler.
11. 11. A method according to any of claims 1 to 10, characterized in that the feed oil is subjected to a desalting treatment prior to the atmospheric distillation step.
12. 12. A method according to any of claims 1 to 10, characterized in that the heavy oil material produced on the basis of the feed oil is oxidized particularly by the oxygen to produce hydrogen, which is used in the hydrotreating steps.
13. 13. A method for the production of fuel oil from the gas turbine from a feed oil with increased yields, characterized in that it comprises: a first separation step for separating the heavy feed oil consisting of the residual atmospheric oil obtained by atmospheric distillation of crude oil and / or heavy oil in a light oil material and a heavy oil material; the first separation step is selected from the group consisting of vacuum distillation, solvent deasphalting, thermal fractionation and steam distillation; and a second hydrotreating step for contacting the light oil material produced in the first separation step with the pressurized hydrogen in the presence of a catalyst, to thereby carry out a removal treatment of the impurities, conducting to obtain a refined oil; the fuel oil of the gas turbine which is the refined oil thus obtained is 4 cSt or less of viscosity at 100 ° C, which contains an alkali metal in an amount of 1 ppm or less, lead in an amount of 1 ppm or less, V in an amount of 0.5 ppm or less, Ca in an amount of 2 ppm or less, and sulfur in an amount of 500 ppm or less, and which is produced in yields of 40% or more based on the oil heavy of the feeding.
14. 14. A method in accordance with the claim 13, characterized in that it further comprises a second separation step for separating the heavy oil material produced in the first separation step into a light oil material and a heavy oil material; the second separation step is selected from the group consisting of solvent deasfallation and thermal fractionation; and a third hydrotreating step for the refining of the light oil material produced in the second separation step, to thereby obtain the refined oil, which is used as the fuel oil of the gas turbine.
15. 15. A method according to claim 13, characterized in that it further comprises a fourth hydrotreating step for contacting the heavy oil material produced in the first separation step with the hydrogen in the presence of a catalyst, to carry out by means of this a treatment of removal of the impurities and the fractionation of a part of the heavy oil material, leading to the obtaining of the refined oil and a heavy oil material; The refined oil produced in the fourth step of hydrotreating is used as the fuel oil of the gas turbine.
16. 16. A method for producing the gas turbine fuel oil from the feed oil with increased yields, characterized in that it comprises: a fifth hydrotreating step for contacting the heavy feed oil consisting of the residual atmospheric oil obtained by the atmospheric distillation of the crude oil and / or the heavy oil with the pressurized hydrogen in the presence of a catalyst, to carry out by means of this a treatment of removal of the impurities and the fractionation as a part of an oil material heavy, leading to obtaining a refined oil and a heavy oil material; a gas turbine fuel oil which is the refined oil thus obtained in the fifth hydrotreating step which is 4 cSt or less in viscosity at 100 ° C, which contains the alkali metal in an amount of 1 ppm or less , the lead in an amount of 1 ppm or less, V in an amount of 0.5 ppm or less, Ca in an amount of 2 ppm or less and sulfur in an amount of 500 ppm or less, and that is produced in yields of 40 % or more based on heavy feed oil.
17. A method according to claim 16, characterized in that it further comprises a third separation step for separating the heavy oil material produced in the fifth hydrotreating step in a light oil material and a heavy oil material; the third separation step is selected from the group consisting of vacuum distillation, solvent deasphalization and thermal fractionation; The light oil material produced in the third separation step is used as the fuel oil of the gas turbine.
18. 18. The fuel oil of the gas turbine, characterized in that it is produced according to a method as defined in any of claims 1 to 17.
19. 19. A method for generating energy, characterized in that it comprises the steps of: driving or operating a gas turbine using the fuel oil of the gas turbine defined in claim 18 as the fuel therefor, to carry out the generation of energy; and using the high temperature exhaust gas discharged from the gas turbine as a heat source for a waste heat recovery boiler and driving a steam turbine by means of the steam generated in said boiler for the recovery of the waste heat , leading to the generation of energy that is carried out. -, PRODUCTION OF THE SAME AND METHOD FOR THE GENERATION OF ENERGY SUMMARY OF THE INVENTION The crude oil is separated into a light oil and a residual oil of normal pressure by an atmospheric distillation and the light oil is brought into contact with a pressurized hydrogen in the presence of a catalyst to effect a first refining of the hydrogenation, a plurality of Light oil grades obtained from an atmospheric distillation column are refined by hydrogenation collectively. The residual oil at normal pressure is separated into a light component and a heavy component, the light component obtained is subjected to a second refining of hydrogenation in the presence of a catalyst, the refined oil (light component) is mixed with the refined oil obtained by the first refining of hydrogenation and the mixed oil is used as a fuel oil of the gas turbine.