JP2000282060A - Gas turbine fuel oil, its production and power generation method - Google Patents

Abstract

PROBLEM TO BE SOLVED: To obtain high quality gas turbine fuel oil at high yield. SOLUTION: Crude oil is subjected to atmospheric distillation so as for light oil to be separated from atmospheric residue and the light oil is subjected to the first hydrogenation processing by being brought into contact with pressurized hydrogen in the presence of a catalyst. Plural kinds of light oil taken out of an atmospheric distillation column are subjected to hydrogenation processing en bloc. The atmospheric residue is divided into light oil and heavy oil, and the light oil is mixed with the above hydrogenated refined oil to be used as gas turbine fuel oil. The heavy oil is divided into light oil and heavy oil, and the light oil may be used for an ingredient of the above blend oil.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a gas turbine fuel oil used as a fuel for gas turbine power generation, a method for producing the same, and a power generation method using gas turbine fuel oil.

[0002]

2. Description of the Related Art Generally, in oil-fired power generation, high-pressure steam is generated using crude oil and / or heavy oil as fuel for a boiler, and power is generated by rotating a steam turbine. However, this system has low power generation efficiency,
At present, high-efficiency large oil-fired boilers are also being developed, but at present the power generation efficiency is only around 40%, and most of the energy is released as greenhouse gas without being recovered. In addition, although a certain amount of SOX is present in the exhaust gas from this system, and although flue gas desulfurization treatment has been performed, a part of the exhaust gas is released to the atmosphere and the environmental impact is becoming serious.

On the other hand, power is generated by turning a gas turbine using natural gas as a heat source, exhaust heat is recovered from high-temperature exhaust gas from the gas turbine, steam is generated, and power is generated by turning the steam turbine. There is a gas turbine combined cycle power generation system. This system has high power generation efficiency and low CO2 emission per power generation unit.
Attention is being paid to OX emissions, which are extremely low.
By the way, if natural gas is used as a raw material, it can be transported from gas fields to power generation facilities by pipeline, or LNG can be stored
After vaporization, it must be burned in a gas turbine, which causes a problem of high equipment cost.

For this reason, a method for producing gas turbine fuel oil using crude oil as a raw material is disclosed in Japanese Patent Application Laid-Open No. 6-2071.
79 and JP-A-6-209600. The technique disclosed in the former publication has a salt content of 0.5 p.
This is a method for producing a gas turbine fuel oil comprising a low-boiling fraction having a sulfur content of 0.05% by weight or less by separating low-sulfur crude oil adjusted to pm or less by atmospheric distillation or vacuum distillation.
Further, the technology of the latter publication uses a waste heat of a gas turbine to heat a low-sulfur crude oil, and then causes hydrogen to act on the low-sulfur crude oil to reduce the content of sulfur and heavy metals in the crude oil to thereby refine the refined crude oil. Is collected and used as fuel oil for gas turbines.

[0005]

However, due to environmental problems, the amount of sulfur compounds in flue gas must be minimized.
This can be solved by installing a flue gas desulfurization unit,
In the case of generating power using gas turbine fuel oil, if a flue gas desulfurization device is provided, the power generation efficiency will be reduced due to pressure loss. Therefore, it is preferable to minimize the sulfur content in the gas turbine fuel oil. In the technique of the above-mentioned publication, fuel oil is obtained only by atmospheric distillation or vacuum distillation, so that the amount to be heated is considerably limited. Therefore,
Light oil, that is, gas turbine fuel oil cannot be obtained in a large amount, and even when Middle Eastern crude oil having relatively low sulfur is used, a yield of only about 40% with respect to crude oil can be obtained. Increasing the amount to be fired to obtain a higher yield will increase the sulfur content.

In general, when the present invention is applied to a crude oil which is easily available and inexpensive and has a high sulfur content, if the same amount of light oil is recovered, the sulfur content in the light oil exceeds the specified value, and as a gas turbine fuel oil, Is inaccurate and the recovery rate must be further reduced, and cannot be employed technically and economically.

On the other hand, the latter publication discloses a technique for generating hydrogen using methanol as a raw material and hydrorefining crude oil using the hydrogen. However, this technique also assumes a low-sulfur crude oil. However, there is a limit to its application to crude oils with high sulfur content. Furthermore, since the target of hydrorefining is to directly hydrotreat crude oil instead of distilled light oil, the process conditions must be adjusted to the heavy oil in crude oil. Also, the reaction time (contact time with the catalyst) must be increased. However, in this case, the cracking of light oil in the crude oil proceeds too much, and a large amount of LPG and the like is contained in the gas turbine fuel oil. As a result, a part of the gas turbine fuel oil is gasified when the gas turbine fuel oil is stored. A tank that can withstand the pressurization is required.
In addition, the reaction temperature and pressure are high, which increases the cost of the structure and materials of the reaction vessel for performing the hydrogenation treatment.In addition, the reaction time is long, the catalyst support becomes large, the reaction vessel becomes large, and the consumption of the catalyst increases. The amount also increases.

The present invention has been made under such circumstances, and an object of the present invention is to provide a technology for producing a gas turbine fuel oil capable of obtaining a gas turbine fuel oil in a high yield relative to a feedstock oil. And a power generation method using the fuel oil.

[0009]

The method for producing gas turbine fuel oil according to the present invention comprises a normal pressure distillation step in which crude oil as a feedstock is subjected to normal pressure distillation to separate a light oil and a normal pressure residue oil. First light hydrogenation treatment in which the light oil obtained in the atmospheric distillation step is brought into contact with pressurized hydrogen in the presence of a catalyst to remove impurities and obtain a refined oil having a sulfur concentration of 150 ppm or less. A first separation step selected from a vacuum distillation step, a solvent removal step, a pyrolysis step, and a steam distillation step for separating the atmospheric residual oil into light oil and heavy oil;
Mixing the light oil obtained in the separation step without hydrotreating at least a part of the light oil with the refined oil to obtain a gas turbine fuel oil. Gas turbine fuel oil has a viscosity of 4
cSt or less, alkali metal is 1 ppm or less, lead is 1 ppm or less, V is 0.5 ppm or less, Ca is 2 ppm or less, and sulfur is 500 ppm or less.

[0010] In the present invention, the second separation step, which is selected from a solvent stripping step and a pyrolysis step, for further separating the heavy oil obtained in the first separation step into a light oil and a heavy oil, is carried out. At least a portion of the light oil obtained in the second separation step without hydrotreating, the light oil not subjected to hydrotreatment obtained in the first separation step, Oil may be mixed to obtain gas turbine fuel oil. In the present invention, when the sulfur content in the feedstock is 1.5% by weight or less, the yield of gas turbine fuel oil based on the feedstock exceeds 60%.

According to the present invention, a light oil which is easily subjected to hydrodesulfurization obtained in the atmospheric distillation step is subjected to thorough hydrotreating, so that a purified oil containing almost no sulfur or metal can be obtained. Therefore, even if the refined oil is mixed with the light oil obtained based on the atmospheric residue, a high-quality gas turbine fuel oil can be obtained. And, since the first hydrotreating step is performed after the atmospheric distillation step, the atmospheric distillation step can boil the light oil without worrying about the amount of sulfur and metal components that enter the light oil. On the other hand, gas turbine fuel oil can be obtained with a high yield. In addition, since the target substance is gas turbine fuel oil, the first hydrotreating step only needs to hydrotreat a plurality of types of light oils obtained from the atmospheric distillation column at once. As a result, equipment costs can be kept low.

If the gas turbine fuel oil thus obtained has a viscosity of 4 cSt or less at 100 ° C., good combustibility is obtained. If the content of metal and sulfur is extremely small as described above, the combustion temperature is low. For example, high-temperature combustion of about 1300 ° C. can be performed.

Further, the present invention provides a second hydrogenation method in which the light oil obtained in the first separation step is brought into contact with pressurized hydrogen in the presence of a catalyst to remove impurities and obtain a purified oil. A treatment step and a second separation step selected from a solvent desorption step and a thermal decomposition step, further separating the heavy oil obtained in the first separation step into a light oil and a heavy oil. And at least a portion of the light oil obtained in the second separation step without hydrotreating, the refined oil obtained in the first hydrotreatment step, and the second oil. May be mixed with the refined oil obtained in the hydrotreating step to obtain a gas turbine fuel oil.

[0014] By performing the second hydrotreating step after the first separation step, the first separation step can be treated so that a large amount of light oil can be obtained without regard to the amount of sulfur or metal. The conditions can be determined, which makes it possible to obtain gas turbine fuel oil with a higher yield based on the feedstock oil. In the present invention, the sulfur content in the base oil is 3% by weight or less, and the yield of gas turbine fuel oil based on the base oil is 70% or more. In this case, the first hydrotreating step and the second hydrotreating step may be shared.

In the above, the present invention also includes gas turbine fuel oil produced by the above-mentioned production method (the production method according to any one of claims 1 to 6).
Further, a step of generating electricity by driving the gas turbine using the gas turbine fuel oil as fuel, and using the high-temperature exhaust gas discharged from the gas turbine as a heat source of an exhaust heat recovery boiler,
The steam generated by the exhaust heat recovery boiler generates steam
The power generation method including the step of driving the bin to generate power is also covered by the rights.

[0016]

DESCRIPTION OF THE PREFERRED EMBODIMENTS FIG. 1 is an explanatory view showing a system for carrying out a method for producing gas turbine fuel oil according to the present invention. Crude oil is used as the feedstock oil 1, and the feedstock oil is first subjected to desalination treatment in the desalination treatment unit 11 under the conditions used in conventional petroleum refining facilities. In this treatment, the raw oil is mixed with water, and the salt and mud are transferred to the aqueous phase.
Removes alkali metals that have an adverse effect on bottles. The desalted raw material oil is sent to the atmospheric distillation column 2 and, for example, 350
It is separated into a light oil 21 having a boiling point lower than 400 ° C and a residual oil (normal pressure residual oil) 22 having a boiling point higher than that. The separated light oil 21 is sent to the first hydrotreating apparatus 3.

Here, the atmospheric distillation column 2 of a general petroleum refining facility
, Since light oils have a high boiling point to a low boiling point, distillates are taken out at every boiling point region, such as kerosene, gasoline, etc. Are provided, and light oils of interest are taken out from the respective outlets.In this embodiment, for example, light oil is taken out at once from the top of the tower, that is, in a state where each fraction is mixed. Removed and sent to the hydrotreating unit. However, as shown in FIG. 2, fractions of each boiling point region are taken out from a plurality of outlets as in a general atmospheric distillation column 2 (in the example of FIG. 2, they are taken out from four outlets), and they are combined. May be sent to the hydrotreating device 3 where the hydrotreating may be performed collectively.

To further explain this point, in the case of batch desulfurization automobile fuel oil production, each of gasoline, kerosene and light oil has a different level of desulfurization, and operating conditions such as temperature, pressure and catalyst are different. On the other hand, in the case of producing gas turbine fuel oil by batch desulfurization of light oil having a boiling point of, for example, lower than 350 ° C., the gas turbine fuel oil only needs to conform to the specifications of the gas turbine fuel oil. It is quite different from the local conditions. Therefore, as described above, the atmospheric distillation column 2
Can be subjected to hydrogenation at once, that is, with a common device.

That is, in the atmospheric distillation process, a plurality of types of light oils having different boiling points can be obtained. However, since the target product is a gas turbine fuel oil, these light oils can be collectively processed by a hydrotreating apparatus. It is possible to reduce the cost of the equipment by performing the batch processing in this manner. Also, the hydrotreating technology applied in the system of the present invention is different from the hydrotreating process in a refinery that produces automobile fuel. For example, in automobile fuel oil, coloring of oil during hydrogenation becomes a problem,
In order to suppress this, low-temperature and high-pressure operation is performed. However, gas turbine fuel oil has no problem with hue, so that high-temperature operation is possible. Therefore, reactor cost can be reduced by low-pressure operation. Costs can be kept low.

Next, the hydrotreating apparatus 3 and its steps (first hydrotreating step) will be described with reference to FIG. 3. Light oil 21 is mixed with pressurized hydrogen gas,
It is supplied into the reaction tower 31 from the upper part of the reaction tower 31. A catalyst layer 32 having a catalyst carried on a carrier is provided in the reaction tower 31, and the light oil 21 and the hydrogen gas pass through the catalyst layer 32 and pass through a liquid feed pipe 33 from the bottom of the reaction tower 31 to a high-pressure tank 34. Flows into. A small amount of heavy metals such as vanadium, nickel, lead and the like contained in the light oil 21, that is, in the hydrocarbon molecule (the metal component is mainly contained in the heavy oil and is very small), and sulfur And nitrogen are light oil 2
When 1 and hydrogen gas pass through the catalyst layer 32, they react with hydrogen to be desorbed from hydrocarbon molecules, metal components are adsorbed on the catalyst surface, and sulfur and nitrogen react with hydrogen to react with hydrogen sulfide,
It becomes ammonia. The alkali metal is dissolved in some water contained in the oil or exists in the form of a salt, but is adsorbed on the catalyst surface.

A mixed fluid of high-pressure gas and oil is discharged from the bottom of the reaction tower 31, and hydrogen gas is separated in a high-pressure tank 34. The hydrogen gas is pressurized by the compressor CP and circulated and supplied into the reaction tower 31. On the other hand, the liquid separated in the high-pressure tank 34 is sent into the low-pressure tank 35 through the pressure regulating valve PV, and the pressure is, for example, 10% to 30%.
%, So that dissolved gases such as hydrogen sulfide and ammonia dissolved in the liquid (oil) evaporate. The liquid thus separated, that is, refined oil, becomes gas turbine fuel oil. 35a is a pump. The gas separated in the low-pressure tank 35 contains hydrogenated compounds such as hydrogen sulfide and ammonia, in addition to unreacted hydrogen gas, and is further generated by cutting off a part of hydrocarbon molecules. Light oils from methane and liquefied petroleum gas fractions to light naphtha (light oil is a lighter component relative to the light oil 21) are also included. From the gas separated in the tank 35, hydrogen sulfide and ammonia contained in the gas are removed in the impurity removing section 36. The impurity removing section 36 is provided with, for example, a tower of an absorbing solution for absorbing hydrogen sulfide and ammonia, and the impurities are removed by passing gas through the tower. The gas from which impurities have been removed is
It is a mixed gas of light oil having a small number of carbon atoms, such as unreacted methane and ethane. The mixed gas 42 is sent to the hydrogen plant 4, and the light oil in the mixed gas 42 is used as a raw material for producing hydrogen gas. A part of the light oil 21 separated by the atmospheric distillation 2 is also sent to the hydrogen plant and used as a raw material for producing hydrogen gas. When the raw material for producing hydrogen gas is limited to heavy oil, the operation may be performed by introducing naphtha from the outside only at the time of starting.

On the other hand, as described above, the hydrogen gas supplied to the reaction tower 31 is circulated and used, but the hydrogen gas in the gas in the circulation path 37 gradually decreases, while the light oil such as methane gradually decreases. To increase. Therefore, in order to prevent the ratio of the hydrogen gas from decreasing, the hydrogen gas 41 is replenished from the hydrogen plant 4 to the circulation path 37, so that the hydrogenation process is reliably performed.

FIG. 4 is a diagram showing a main part of the hydrogen plant 4. This hydrogen plant 4 has a combustion furnace 4 for burning fuel gas.
3, a light pipe such as methane and steam are passed through the reaction pipe 44, and the light oil is steam-reformed to produce hydrogen and by-produced carbon monoxide.
Then, carbon monoxide is removed from this gas to obtain hydrogen gas. For the removal treatment (purification) performed here, for example, PSA (pressure fluctuation adsorption separation method), TSA (temperature fluctuation adsorption separation method), cryogenic separation method, membrane separation method, or the like can be used.

Here, in the first hydrotreating step of the present invention and the second hydrotreating step performed in the embodiment described later, the sulfur compound is brought into contact with pressurized hydrogen in the presence of a catalyst. Its main purpose is hydrodesulfurization to remove impurities.

The process (first hydrotreating step) performed in the first hydrotreating apparatus 3 will be described. In the conventional petroleum refining, naphtha, kerosene light oil, and the like in a light oil fraction are separately targeted. In contrast, in the present invention, all the fractions distilled by atmospheric distillation are subjected to the hydrotreating at once. Therefore, the amount of hydrotreating is greatly increased, which is greatly different from the conventional case. The conditions such as the pressure of hydrogen gas and the reaction temperature of the hydrogenation treatment are 340 to 420 ° C., the pressure of hydrogen gas is 30 kg / cm 2 to 80 kg / cm 2, and the LHVS (liqu
(id hourly space velocity) can be selected from 0.5 to 6 hr-1 and the sulfur concentration of the refined oil is preferably set to 150 ppm or less. As the catalyst, a conventionally known hydrotreating catalyst can be arbitrarily selected, but a catalyst in which sulfides of Ni, Mo, and Co are supported on alumina is preferable. Such a technique is a technique being developed to achieve an ultra-deep desulfurization level (50 ppm) of a light oil for automobiles. In the present invention, various techniques are applied to a wide range of distillate oils from naphtha to kerosene light oil by applying the technique. This is to carry out ultra-deep desulfurization of 30 to 150 ppm in the oil type.

On the other hand, the residual oil (normal pressure residual oil) 22 separated in the atmospheric distillation column 2 is separated in a first separation step and separated into light oil and heavy oil. This separation step can be, for example, a vacuum distillation step. In this case, the residual oil is sent to the vacuum distillation column 5 where it is a light component among the atmospheric residual oils, for example, a light oil (low-pressure light oil) 51 whose boiling point at normal pressure is lower than 565 ° C. and a heavy component. ,
It is separated into heavy oil (vacuum residual oil) 52 whose boiling point exceeds normal pressure.

The light oil 51 is not hydrotreated.
At least a part thereof is mixed with the refined oil 30 obtained in the first hydrotreating step 3 (mixing step),
It becomes bottle fuel oil. The mixing ratio depends on the feedstock,
Regarding the properties of gas turbine fuel oil, viscosity is 4 cSt or less at 100 ° C, alkali metal is 1 ppm or less, lead is 1 ppm
Hereinafter, mixing is performed so that V is 0.5 ppm or less, Ca is 2 ppm or less, and sulfur is 500 ppm or less. The heavy oil (vacuum residue) 52 is used as a heavy oil feedstock or boiler fuel oil after its viscosity is adjusted as required.

According to the above-described embodiment, since the hydrogenation treatment is performed after the atmospheric pressure distillation step, it is possible to heat up without worrying about the amount of sulfur or heavy metal. Squeezing can be performed, and as a result, a large amount of refined oil containing almost no sulfur can be obtained. On the other hand, since the light oil 51 obtained through the vacuum distillation has not been subjected to hydrogenation treatment and has a high sulfur concentration, the amount of the light oil 51 is adjusted according to the sulfur concentration, and the light oil 51 is mixed with the refined oil 30. Thus, a gas turbine fuel oil satisfying the above-mentioned component rules can be obtained.

Since the light oil 51 separated from the normal pressure residual oil is not subjected to the hydrotreating but at least a part thereof is mixed with the refined oil 30, the first hydrotreating apparatus 3 is used as the hydrotreating apparatus 3. Equipment costs can be kept low because only processing is required. In addition, when compared with the example in which the light oil 51 is supplied to the first hydrotreating apparatus 3 as described later, since the hydrotreating conditions must be adjusted to the properties of the light oil 51, the reaction of temperature, pressure, etc. Due to the stricter conditions, the cost of equipment is
The embodiment is more advantageous. Regarding the yield of gas turbine fuel oil, the sulfur concentration of the feed oil was 0.8% by weight.
If low sulfur crudes are used, a yield of 70% by weight or more is obtained. The sulfur concentration of the feedstock is 0.8% by weight.
As described above, when the content is 1.5% by weight or less, a yield exceeding 60% by weight is obtained.

Since the crude oil is not hydrotreated as it is, but the light oil is hydrotreated after the distillation step, the reaction conditions may be adjusted to that of the light oil. It is not necessary, the reaction time is short, and the equipment can be simplified accordingly. Further, since it is intended for gas turbine fuel oil, as described above, without performing hydrotreating on each fraction obtained in the distillation step,
These can be subjected to hydrogenation at once, and thus hydrogenation can be performed by a simple process as a whole even though hydrogenation is performed.

In the present invention, the method of performing the first separation step of separating the residual oil 22 of the atmospheric distillation apparatus 2 is not limited to vacuum distillation, but may be, for example, a steam distillation method, a solvent removal method, or a method of removing the residual oil 22. For example, a thermal decomposition method of heating to 430 to 490 ° C. and cutting hydrocarbon molecules by thermal energy to obtain light oil and heavy oil may be used.

The present invention also relates to a method for producing heavy oil obtained in the first separation step when the sulfur concentration of the feedstock oil is as low as 0.5% by weight or less. And the light oil is mixed with the refined oil and the light oil 51.
(Mixing Step) Gas turbine fuel oil may be obtained. FIG. 5 is a diagram showing such an embodiment.
Vacuum distillation is carried out as a separation step, and the heavy fraction (vacuum residue oil) 52 is subjected to solvent removal as a second separation step.
An example is shown in which a (solvent extraction) step is performed.

The heavy oil (vacuum residue oil) 52 separated in the vacuum distillation column 5 is separated by a solvent degreasing unit (solvent extraction unit) 6 into a degreasing oil 61 which is a light oil and a degreasing residue which is a heavy oil. Oil 6
And 2. In this separation, for example, the vacuum residue 52 and the solvent are supplied from the upper and lower portions of the column, respectively, and they are brought into countercurrent contact with each other, and light oil and heavy oil in the vacuum residue 52 are separated by the difference in solubility in the solvent. It is done by doing.

At least a part of the separated deoiled oil (light oil) 61 is mixed with the light oil 51 from the vacuum distillation column 5 and the refined oil 30 and used as a gas turbine fuel oil. After the viscosity of the removed residual oil 62 is adjusted as required, it is used as a heavy oil feedstock or a boiler fuel oil. Note that the second separation step may be the above-described thermal decomposition step. Further, according to the present invention, when the sulfur concentration of the feed oil is as high as 1.7% by weight, for example, in the embodiment of FIG. 5, as shown in FIG. The apparatus 7 is installed, and the light oil 51 (decompressed light oil) is sent to the second hydrotreating apparatus 7 to perform the hydrotreating apparatus (second hydrotreating step), and the refined oil 70 that has been hydrotreated
May be mixed with at least a part of, for example, the light oil 61 obtained in the second separation step and the refined oil 30 (mixing step) and used as a gas turbine fuel oil.

According to such an embodiment, the light oil 5
1 (decompressed gas oil) is also hydrotreated,
For example, with respect to the light oil 61 obtained in the second separation step, the gas turbine fuel oil having a sulfur concentration falling within a specified value can be obtained at a high yield by mixing with the refined oils 30 and 70 without performing the hydrogenation treatment. Can be obtained at In this case, the yield of the gas turbine fuel oil is 80% by weight or more when a low sulfur crude oil having a low sulfur concentration of less than 2% by weight is used as a feed oil. Also, if the sulfur concentration of the feed oil is 2
When the amount is from 3% by weight to 3% by weight, a yield of 70% by weight or more is obtained.

The conditions such as the pressure of hydrogen gas, the reaction temperature and the like in the second hydrotreating apparatus 7 are from 360 ° C. to 420 ° C. and the pressure of hydrogen gas 3
0kg / cm2 ~ 100kg / cm2, LHVS (liquid
hourly space velocity) can be selected from 0.1 to 3 hr -1, and the sulfur concentration of the refined oil is preferably, for example, 500 ppm or less. Further, the present invention provides a method for separately hydrogenating the light oil 21 obtained in the atmospheric distillation column 2 and the light oil (decompressed light oil) 51 obtained in the vacuum distillation column 5 as in the embodiment of FIG. Instead of processing with a processing device, these may be mixed and subjected to hydrogenation in the same hydroprocessing device 8 as shown in FIG. That is, in this case, the first hydrotreating apparatus 3
This means that the second hydrotreating apparatus 7 is shared.
Generally, the reaction conditions for the hydrotreating are set in accordance with the heavy oil in the feedstock. In this example, the heavy oil is light oil (reduced light oil) 51.
Is equivalent to Therefore, the light oil 21 and the reduced light oil 5
By reducing the ratio of the light oil 21 to the weight ratio (capacity ratio) to 1 and treating them collectively, the light oil hydrotreating apparatus can be omitted, and the cost can be reduced.
If the ratio of the light oil 21 is high (that is, the reduced light oil 51
Is low), the reaction conditions are set in accordance with a small amount of heavy oil (corresponding to the reduced pressure light oil 51), so that the design value of the reactor becomes strict and the economic effect is hardly obtained. On the other hand, if the refined light oil 51 is refined in accordance with the reaction conditions, the refining degree of the light oil is greatly improved. When the light oil 51 obtained in the vacuum distillation column 5 is subjected to hydrogenation treatment, heavy oil may be supplied to the vacuum distillation column 5 as shown by a dotted line in FIGS. 6 and 7. Such a supply does not affect a series of steps performed by supplying the crude oil to the atmospheric distillation column 2 of the present invention. The mixed oil (gas turbine oil) obtained as described above is distilled at, for example, 350 ° C. in an atmospheric pressure distillation column (not shown) to produce a light gas turbine fuel oil and a heavier gas turbine fuel oil. Bottle fuel oil may be obtained. In the present invention, the heavy oil obtained in the above-described first separation step and / or second separation step is partially oxidized with oxygen gas to generate hydrogen, and the hydrogen is used in a hydrotreating apparatus. You may do so. The gas turbine fuel oil obtained by the present invention can be used, for example, for power generation, and an example is shown in FIG. The gas turbine fuel oil is burned by a combustion nozzle, and the combustion gas drives the gas turbine 201, so that electric power is extracted from the generator 202. On the other hand, the high-temperature exhaust gas discharged from the gas turbine 201 is discharged to the exhaust heat recovery boiler 2.
03 and generates steam by the heat of the exhaust gas. The steam drives the steam turbine 204 to extract power from the generator 205. If power is generated in this manner, the exhaust heat of the gas turbine fuel oil can be effectively used, and power generation can be performed with high efficiency.

(Example 1) The UAE Murban crude oil (sulfur concentration: 0.7
(8% by weight). After 100 weight units of crude oil undergoes a desalting process, it is separated into a light oil (75 weight units) having a boiling point lower than 380 ° C and a heavy oil (25 weight units) having a higher boiling point by an atmospheric distillation process. The pressure of the hydrogen gas in the first hydrotreating step is 50 kg / c
m2, LHSV 1hr-1 and sulfur concentration 60pp
m deep desulfurized refined oil was obtained. In the first distillation step, a vacuum distillation step, a light oil having a boiling point (boiling point at normal pressure) having a sulfur concentration of 8500 ppm lower than 480 ° C. (4 weight units)
And heavy oil having a higher boiling point. The light oil obtained in this vacuum distillation step was mixed with the gas turbine fuel oil obtained in the first hydrotreating. As a whole gas turbine fuel oil, the recovery rate is 79 weight units, and no alkali metal, alkaline earth metal, vanadium, and lead are detected.
The sulfur concentration is 490 ppm and the viscosity is 0.1 at 100 ° C.
Production of 4 cSt gas turbine fuel oil has become possible.

The simulation was performed assuming that all the energy from the crude oil was converted to electric power (gas turbine and boiler power generation). The internal consumption rate at the refinery plant is 4
%, Combined cycle gas turbine power generation efficiency 4
9% and boiler power generation efficiency were set to 38%. Under the above conditions, supply of crude oil to the refinery plant
When the final power recovery amount was calculated using 0 units, it was possible to recover 45.2 units of power energy in terms of calorific value.

(Comparative Example 1) As in Example 1, the UAE M
A gas turbine fuel oil was produced using urban crude oil according to Japanese Patent Application Laid-Open No. 6-207179. According to the same report, a gas turbine fuel oil having a sulfur concentration of 0.05 wt% or less is produced by using a low-sulfur crude oil whose salt concentration is adjusted to 0.5 ppm or less as a raw material by a distillation method. Gas turbine fuel oil is limited to kerosene fractions from light naphtha up to a boiling point of 230 ° C. No alkali metal, alkaline earth metal, V and lead are detected, the sulfur concentration is about 490 ppm, and the viscosity is 1
Although the quality was as high as 0.1 cSt at 00 ° C., the yield of the gas turbine fuel oil relative to the feed oil was a low recovery of 39%.

A simulation was performed under the same conditions as in Example 1 except that the in-house consumption rate in the refinery plant was 3%. The crude oil supply to the refinery plant is 1 calorie equivalent
When the final power recovery amount was calculated as 00 units,
Only 41.1 units of power energy could be recovered in terms of calorific value, which proved to be significantly inferior to the present invention from the viewpoint of effective energy utilization.

Example 2 Arabian light crude oil (sulfur concentration: 1.77 watts) was obtained by the process of the present invention shown in FIG.
(%), turbine oil production was attempted. 100 weight units of crude oil undergoes a desalting process and then has a boiling point of 36 in an atmospheric distillation process.
Light oil (60 weight units) lower than 0 ° C. and heavy oil (40 weight units) having a higher boiling point are separated, and the pressure of hydrogen gas in the first hydrotreating step is reduced to 45 kg / cm.
2. A LHSV of 2 hr-1 was obtained to obtain a deep desulfurized refined oil having a sulfur concentration of 50 ppm. In the first distillation step, ie, a vacuum distillation step, a vacuum gas oil (23 weight units) having a boiling point (boiling point at normal pressure) lower than 560 ° C. and a heavy oil (17 weight units) having a higher boiling point than that are obtained. separated. In a second hydrorefining unit, the pressure of the reduced pressure gas oil is reduced to 75 k
g / cm 2, LHSV 0.8 hr −1, and a desulfurized refined oil having a sulfur concentration of 300 ppm was obtained. Further, this heavy oil is subjected to SDA as a second separation step, and the sulfur concentration is 1000 p.
The pm degreasing oil (3 weight units) was recovered. The deoiled oil, the light oil obtained in the second hydrotreating, and the gas turbine fuel oil obtained in the first hydrotreating were mixed. The recovery rate of the gas turbine oil as a whole was 85 weight units, and 0.7 ppm of alkali metal, 0.8 ppm of Ca, 0.5 ppm of vanadium, and no lead were detected.
It became possible to produce a gas turbine oil having 0 ppm and a viscosity of 0.8 cSt at 100 ° C.

The simulation was performed assuming that all the energy from crude oil was converted to electric power (gas turbine and boiler power generation). The on-site consumption rate at the refinery plant is 5
%, Combined cycle gas turbine power generation efficiency 4
9% and boiler power generation efficiency were set to 38%. Under the above conditions, supply of crude oil to the refinery plant
When the final power recovery amount was calculated using 0 units, it was possible to recover 45.1 units of energy in terms of calorific value.

Comparative Example 2 A gas turbine fuel oil was produced in the same manner as in Example 1 by using Arabian light oil as a crude oil according to JP-A-6-207179. Gas turbine fuel oil from this report is limited to kerosene fractions from light naphtha with boiling point range up to 245 ° C, alkali metal, alkaline earth metal, V and lead are not detected and sulfur concentration is about 470p
pm and a viscosity of 0.3 cSt at 100 ° C., but the gas turbine fuel oil yield based on the feed oil was 24%
And an extremely low recovery rate.

The simulation was performed under the same conditions as in Example 1 except that the in-house consumption rate in the refinery plant was 3%. The crude oil supply to the refinery plant is 1 calorie equivalent
When the final power recovery amount was calculated as 00 units,
It was found that only 39.5 units of power energy could be recovered in calorie conversion, which was significantly inferior to the present invention from the viewpoint of effective energy utilization.

[0045]

As described above, according to the present invention, crude oil is subjected to normal pressure distillation, the light oil is subjected to hydrogenation treatment to obtain a refined oil, and the normal pressure residue oil is subjected to separation treatment. The gas turbine fuel oil is obtained by mixing at least a part of the obtained light oil and the refined oil. Further, the light oil obtained by performing the first separation step on the atmospheric residual oil is subjected to hydrogenation treatment, and the refined oil obtained by the hydrogenation treatment and the refined oil obtained by hydrotreating the atmospheric pressure gas oil And at least a portion of light oil obtained by further separating from the heavy oil obtained in the first separation step to obtain gas turbine fuel oil. It can be obtained in yield.

[Brief description of the drawings]

FIG. 1 is an explanatory diagram showing an example of a system for implementing a method of the present invention.

FIG. 2 is an explanatory view showing another example of a method for removing light oil from an atmospheric distillation column in the above system.

FIG. 3 is an explanatory diagram illustrating an example of a hydrotreating apparatus.

FIG. 4 is an explanatory diagram showing an example of a main part of a hydrogen plant.

FIG. 5 is an explanatory diagram showing another example of a system for implementing the method of the present invention.

FIG. 6 is an explanatory diagram showing still another example of a system for implementing the method of the present invention.

FIG. 7 is an explanatory diagram showing still another example of a system for implementing the method of the present invention.

FIG. 8 is an explanatory diagram showing an example of a method for using gas turbine fuel oil obtained in the present invention.

[Explanation of symbols]

 DESCRIPTION OF SYMBOLS 1 Raw material oil 11 Desalination processing part 2 Normal pressure distillation column 21 Light oil 22 Normal pressure residue oil 3 First hydrotreating unit 4 Hydrogen plant 5 Vacuum distillation column 6 Solvent dewatering device 7 Second hydrotreating device 60 Third Hydrotreating Device 201 Gas Turbine 203 Exhaust Heat Recovery Boiler 204 Steam Turbine

──────────────────────────────────────────────────の Continued on the front page (51) Int.Cl. ⁷ Identification symbol FI Theme coat ゛ (Reference) C10L 1/04 C10L 1/04 (72) Inventor Yoshinori Masuko 2-3-1 Minato Mirai, Nishi-ku, Yokohama-shi, Kanagawa Nikko (72) Inventor Shinichi Tokuda 2-3-1 Minatomirai, Nishi-ku, Yokohama-shi, Kanagawa Japan JGC Corporation F-term (reference) 4H029 AA11 AB01 AB05 AC04 DA01 DA02 DA05 DA09

Claims (8)

[Claims] 1. An atmospheric distillation step in which a crude oil as a feed oil is subjected to atmospheric distillation to separate a light oil and an atmospheric residual oil, and the light oil obtained in the atmospheric distillation step is collectively used as a catalyst. A first hydrotreating step of contacting with pressurized hydrogen in the presence to perform a de-impurity treatment to obtain a refined oil having a sulfur concentration of 150 ppm or less, and converting the normal pressure residue oil into light oil and heavy oil Separating, a first separation step selected from a reduced pressure distillation step, a solvent removal step, a thermal decomposition step and a steam distillation step, and at least without subjecting the light oil obtained in the first separation step to a hydrogenation treatment. A mixing step of mixing a part thereof with the refined oil to obtain a gas turbine fuel oil. The gas turbine fuel oil obtained in the mixing step has a viscosity of 4 cSt or less at 100 ° C. and an alkali metal. 1 ppm or less,
Lead is 1 ppm or less, V is 0.5 ppm or less, Ca is 2 pp
m and a sulfur content of 500 ppm or less. 2. An atmospheric distillation step in which crude oil as a feed oil is subjected to atmospheric distillation to separate it into a light oil and an atmospheric residue, and the light oil obtained in the atmospheric distillation step is collectively used as a catalyst. A first hydrotreating step of contacting with pressurized hydrogen in the presence to perform a de-impurity treatment to obtain a refined oil having a sulfur concentration of 150 ppm or less, and converting the normal-pressure residue oil into a light oil and a heavy oil Separating, a first separation step selected from a vacuum distillation step, a solvent removal step, a thermal decomposition step and a steam distillation step; and the heavy oil obtained in the first separation step is further combined with a light oil and a heavy oil Separating into oil, a second separation step selected from a solvent removal step and a thermal decomposition step, and at least a part of the light oil obtained in the second separation step without hydrotreating and The light oil not subjected to hydrotreating obtained in the first separation step and the refined oil are combined with each other. Combined Antofagasta and - comprises a mixing step of obtaining a bottle fuel oil, the gas turbine fuel oil obtained in this mixing step, viscosity of 4cSt less at 100 ° C., the alkali metal is 1ppm or less,
Lead is 1 ppm or less, V is 0.5 ppm or less, Ca is 2 pp
m and a sulfur content of 500 ppm or less. 3. The method according to claim 1, wherein the sulfur content in the feedstock is 1.5% by weight or less, and the yield of gas turbine fuel oil based on the feedstock exceeds 60%.
A method for producing the gas turbine fuel oil according to the above. 4. An atmospheric distillation step in which a crude oil as a feed oil is subjected to atmospheric distillation to separate it into a light oil and an atmospheric residue, and the light oil obtained in the atmospheric distillation step is collectively used as a catalyst. A first hydrotreating step of contacting with pressurized hydrogen in the presence to perform a de-impurity treatment to obtain a refined oil having a sulfur concentration of 150 ppm or less, and converting the normal pressure residue oil into light oil and heavy oil Separating, a first separation step selected from a vacuum distillation step, a solvent removal step, a thermal decomposition step and a steam distillation step; and pressurizing the light oil obtained in the first separation step in the presence of a catalyst. A second hydrotreating step of obtaining a refined oil by performing a de-impurity treatment by bringing the heavy oil into contact with the hydrogen, and further separating the heavy oil obtained in the first separation step into a light oil and a heavy oil A second separation step selected from a solvent stripping step and a thermal decomposition step, and the second separation step The light oil obtained by the above-mentioned method is subjected to at least a part thereof without hydrotreating, the refined oil obtained in the first hydrotreating step and the refined oil obtained in the second hydrotreating step. A mixing step of mixing to obtain a gas turbine fuel oil. The gas turbine fuel oil obtained in this mixing step has a viscosity of 4 cSt or less at 100 ° C., an alkali metal of 1 ppm or less,
Lead is 1 ppm or less, V is 0.5 ppm or less, Ca is 2 pp
m and a sulfur content of 500 ppm or less. 5. The process according to claim 4, wherein the first hydrotreating step and the second hydrotreating step are common steps.
A method for producing the gas turbine fuel oil according to the above. 6. The feedstock according to claim 4, wherein the sulfur content in the feedstock is 3.0% by weight or less, and the yield of gas turbine fuel oil to the feedstock is 70% or more. For producing gas turbine fuel oil. 7. A gas turbine fuel oil produced by the production method according to claim 1. 8. A step of generating electricity by driving the gas turbine using the gas turbine fuel oil produced in claim 7 as a fuel, and providing a high-temperature exhaust gas discharged from the gas turbine to an exhaust heat recovery boiler. Generating a power by driving a steam turbine with steam generated by the exhaust heat recovery boiler as a heat source.