WO2000026325A1 - Huile combustible pour turbine a gaz, son procede de production et procede de production d'energie - Google Patents
Huile combustible pour turbine a gaz, son procede de production et procede de production d'energie Download PDFInfo
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- WO2000026325A1 WO2000026325A1 PCT/JP1999/004927 JP9904927W WO0026325A1 WO 2000026325 A1 WO2000026325 A1 WO 2000026325A1 JP 9904927 W JP9904927 W JP 9904927W WO 0026325 A1 WO0026325 A1 WO 0026325A1
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- oil
- gas turbine
- turbine fuel
- fuel oil
- heavy
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/14—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural parallel stages only
- C10G65/16—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural parallel stages only including only refining steps
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1033—Oil well production fluids
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/205—Metal content
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/302—Viscosity
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4025—Yield
Definitions
- the present invention relates to a gas turbine fuel oil, a method for producing the same, and a power generation method.
- the present invention relates to, for example, 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 the gas turbine fuel oil.
- 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.
- This is a method for recovering oil and using it as fuel oil for gas turbines.
- the present invention has been made under such circumstances, and a technology for producing a gas turbine fuel oil capable of obtaining a gas turbine fuel oil at a high yield with respect to a feedstock oil, and the use of the fuel oil.
- the purpose of the present invention is to provide a power generation method.
- the method for producing gas turbine fuel oil of the present invention is obtained by 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 residual oil; A first hydrotreating step in which the light oil is collectively brought into contact with pressurized hydrogen in the presence of a catalyst to remove impurities and obtain a refined oil; A first oil separation step selected from a vacuum distillation step, a solvent removal step, a thermal cracking step and a steam distillation step, and the light oil obtained in the first separation step in the presence of a catalyst. A second hydrogenation step of performing a de-impurity treatment by contacting with hydrogen under pressure in the presence to obtain a refined oil, wherein the first and second hydrogenation steps are performed.
- Gas turbine fuel oil has a viscosity of 4 cSt or less at 100 ° C, an alkali metal of 1 ppm or less, and a lead of 1 ppm or less.
- V is 0. 5 p p m or less, C a following 2 p p m, sulfur is not more than 5 0 0 p p m, and wherein the yield with respect to the feed oil is 6 more than 5%.
- the present invention further comprises a second separation step selected from a solvent removal step and a pyrolysis step, wherein the heavy oil obtained in the first separation step is further separated into light oil and heavy oil,
- the light oil obtained in the second separation step may be subjected to a third hydrotreating step.
- at least two of the first hydrotreating step, the second hydrotreating step, and the third hydrotreating step can be a common step. According to the present invention, since the first hydrotreating step is performed after the normal pressure distillation step, it is possible to boil up the light pressure oil without worrying about the amount of sulfur or metal that enters the light oil.
- the processing conditions are determined so that even in the first separation step, a large amount of light oil can be obtained without regard to the amount of sulfur and metal. Can be For this reason, gas turbine fuel oil can be obtained with a high yield based on the feedstock oil.
- the first hydrotreating step since the target substance is gas turbine fuel oil, the first hydrotreating step only needs to hydrotreat a plurality of types of light oil obtained from the atmospheric distillation column at once, and by doing so, Equipment costs can be kept low.
- the viscosity of the gas turbine fuel oil is 4 cSt or less at 100 ° C, the combustibility is good, and if the metal and sulfur contents are extremely small as described above, the combustion temperature For example, high-temperature combustion of about 130 ° C. can be performed.
- the present invention also provides a heavy oil obtained in the first separation step, which is brought into contact with pressurized hydrogen in the presence of a catalyst to remove impurities and to partially decompose the heavy oil to obtain a purified oil And a fourth hydrotreating step for obtaining heavy oil.
- the refined oil obtained in the fourth hydrotreating step may be used as a gas turbine fuel oil.
- the above-mentioned first separation step may be replaced with a hydrotreating step (fifth hydrotreating step), in which case the heavy oil obtained in the fifth hydrotreating step is further lightened.
- a hydrotreating step (fifth hydrotreating step), in which case the heavy oil obtained in the fifth hydrotreating step is further lightened.
- It includes a third separation step selected from a distillation step, a solvent removal step, and a pyrolysis step in which oil and heavy oil are separated, and the light oil obtained in this third separation step is used as gas turbine fuel oil. May be used.
- the gas turbine fuel oil obtained as described above is further distilled at normal pressure to obtain a light gas turbine fuel oil and a gas turbine fuel oil heavier than the gas turbine fuel oil. Is also good.
- the heavy oil obtained in the final separation step or the heavy oil obtained in the fourth hydrotreating step among the above separation steps can be used as fuel oil for a boiler.
- the raw material of hydrogen is not particularly limited, but the heavy oil obtained based on the raw oil, for example, the heavy oil obtained in the first separation step is partially oxidized by oxygen. Hydrogen is generated, and this hydrogen can be used as a raw material used in the hydrotreating process.
- the present invention may also use a heavy crude oil composed of an atmospheric residual oil obtained by atmospheric distillation of crude oil and / or heavy oil as a starting material.
- a first separation step selected from vacuum distillation, solvent removal, thermal cracking, and steam distillation steps for separating light oil and heavy oil, and a first separation step.
- the method includes a second separation step selected from solvent desorption and thermal cracking steps for further separating the heavy oil obtained in the first separation step into light oil and heavy oil.
- the light oil obtained in the second separation step may be subjected to a third hydrotreating step to obtain a refined oil, which may be used as a gas turbine fuel oil.
- the heavy oil obtained in the first separation step is brought into contact with pressurized hydrogen in the presence of a catalyst to perform a de-impurity treatment, and a part of the heavy oil is decomposed to obtain a purified oil and heavy oil.
- It may include a fourth hydrotreating step for obtaining oil and the refined oil obtained in the fourth hydrotreating step may be used as a gas turbine fuel oil.
- a heavy crude oil consisting of atmospheric residual oil obtained by distilling crude oil under normal pressure and Z or heavy oil is brought into contact with pressurized hydrogen in the presence of a catalyst to carry out a de-impurity treatment and a heavy impurity treatment.
- Gas turbine fuel oil which is a refined oil obtained in the fifth hydrotreating step, includes a fifth hydrotreating step of decomposing a part of the heavy oil to obtain a refined oil and a heavy oil.
- the heavy oil obtained in the fifth hydrotreating step is further separated into light oil and heavy oil, and the third separation is selected from vacuum distillation, solvent removal, and pyrolysis.
- the light oil obtained in the third separation step may be used as gas turbine fuel oil!
- crude oil is subjected to normal pressure distillation, the light oil is subjected to hydrogenation treatment, and the normal pressure residue is subjected to separation treatment or hydrogenation treatment. Hydrogen treatment is performed, and the refined oil is used as gas turbine fuel oil. Therefore, high quality gas turbine fuel oil can be obtained with high yield.
- the present invention includes a gas turbine fuel oil produced by the above-described production method, which is also included in the scope of rights, further comprising a step of driving a gas turbine using the gas turbine fuel oil as a fuel to generate electric power;
- FIG. 1 is an explanatory diagram showing an example of a system for carrying out the method of the present invention.
- FIG. 2 is an explanatory diagram showing another example of a method for removing light oil from an atmospheric distillation column in the above system.
- 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 view showing still another example of the system for implementing the method of the present invention
- FIG. 7 is an explanatory view showing still another example of the system for implementing the method of the present invention, FIG. FIG.
- FIG. 9 is an explanatory diagram showing another example of the system for implementing the method of the present invention other than the above example.
- FIG. 9 is a diagram showing the system for implementing the method of the present invention.
- FIG. 10 is an explanatory diagram showing another example, and
- FIG. 10 is an explanatory diagram showing another example other than the above example of the system for implementing the method of the present invention.
- FIG. 11 is a diagram showing the method of the present invention.
- FIG. 12 is an explanatory view showing another example of the system for carrying out the present invention other than the above example.
- FIG. 12 is an explanatory view showing an outline of an example of the partial oxidation equipment shown in FIG. 10, and
- FIG. 13 is the present invention.
- FIG. 3 is an explanatory diagram showing an example of a method of using gas turbine fuel oil obtained in Step (a).
- FIG. 1 is an explanatory view showing a system for carrying out the method for producing gas turbine fuel oil of the present invention.
- the first to fifth hydrotreating steps are described according to the stage of performing the force treatment in which the hydrotreating step is performed.
- the gas turbine fuel oil obtained in these hydrotreating steps is generally used as a mixture, and in each of the embodiments, the power will be described by taking the case of mixing as an example. It may be used as a gas turbine fuel oil.
- Crude oil is used as the feedstock oil 1.
- the feedstock oil is first desalinated in the desalination unit 11 under the conditions used in conventional oil refining facilities. This process mixes the feedstock oil with water, transfers salt and mud to the aqueous phase, and removes alkali metals that can adversely affect the gas turbine.
- the desalted feedstock is sent to the atmospheric distillation column 2, for example, a light oil 21 with a boiling point lower than 34 ° C to 37 ° C and a residual oil with a boiling point higher than that (atmospheric pressure). (Residual oil).
- the separated light oil 21 is sent to the first hydrotreating unit 3.
- distillates in 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 these are combined to form hydrogen.
- processing apparatus sends to 3, it may be subjected to hydrotreating in a lump here c
- 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, and it is suppressed. Therefore, it can be operated at low temperature and high pressure, but the gas turbine fuel oil has no problem with the hue, so it can be operated at high temperature, and thus the cost of the reactor can be reduced by the low pressure of 313 ⁇ 4. be able to.
- Light metals such as vanadium, nickel, lead, and other heavy metals contained in light oil 21 that contain hydrocarbon molecules (metals are extremely small because they are mainly contained in heavy oil )
- sulfur and nitrogen Means that when light oil 21 and hydrogen gas pass through the catalyst layer 32, they react with hydrogen and are desorbed from hydrocarbon molecules, metals are adsorbed on the catalyst surface, and sulfur and nitrogen react with hydrogen.
- the alkali metal is dissolved in some of the 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 for example, 30 to 80 kg / cm 2 is discharged from the bottom of the reaction tower 31, and hydrogen gas is separated in the high-pressure tank 34.
- the hydrogen gas is pressurized by the compressor CP and circulated into the reaction tower 31.
- the liquid separated in the high-pressure tank 34 is sent to the low-pressure tank 35 via the pressure regulating valve PV, and the pressure is reduced, for example, by about 10% to 30%.
- Liquid gases such as hydrogen sulfide and ammonia dissolved therein evaporate.
- 3 5a 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.
- Light oil from generated methane and liquefied petroleum gas fraction to light naphtha (Light oil here includes J, which is a lighter component than light oil 21.
- Tank 3 The gas separated in 5 is subjected to an impurity removing section 36 to remove hydrogen sulfide and ammonia contained in the gas.
- the impurity removing section 36 is provided with a layer of an absorbing solution for absorbing, for example, hydrogen sulfide and ammonia, and the impurities are removed by passing gas through the layer.
- the gas from which the impurities have been removed is unreacted hydrogen gas.
- a mixed gas of light oil having a small number of carbon atoms, such as methane 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.
- the hydrogen gas supplied to the reaction tower 31 is circulated and used.
- the amount of hydrogen gas in the gas in the circuit 37 gradually decreases, while light oil such as methane gradually increases.
- hydrogen gas 41 is replenished from the hydrogen plant 4 to the circulation path 37 to ensure that the hydrogenation treatment is performed.
- FIG. 4 is a diagram showing a main part of the hydrogen plant 4.
- This hydrogen plant 4 is provided with a reaction tube 44 in a combustion furnace 43 for burning fuel gas, and passes light oil such as methane and steam through the reaction tube 44 to convert the light oil into steam. And produce hydrogen together with carbon monoxide. Then, carbon monoxide and unreacted light oil are converted or removed from this gas to obtain hydrogen gas.
- PSA pressure fluctuation adsorption separation method
- TSA temperature fluctuation adsorption separation method
- cryogenic separation method or membrane separation method can be used for the removal treatment (purification) performed here.
- the first to fifth hydrotreating steps of the present invention are carried out by bringing into contact with pressurized hydrogen in the presence of a catalyst, 1) hydrodesulfurization for the purpose of removing impurities such as sulfur compounds, 2)
- the first hydrotreating step may include any of the following reactions: hydrorefining for the purpose of improving properties by the saturation of unsaturated hydrocarbons, etc., and 3) hydrocracking for the purpose of light-weight oil.
- the main purpose of the above is 1), the second and third hydrotreating steps are 1) and 2) as the main purpose, and the fourth and fifth hydrotreating steps are any of 1) to 3). Is also its main purpose.
- the naphtha, kerosene and oil etc. in the light oil fraction are separately treated to hydrotreat a fraction with a narrow boiling point range.
- all of the fractions distilled by atmospheric distillation are subjected to hydrotreating at once. Therefore, the amount of hydrotreating is greatly increased, which is significantly different from the conventional method.
- a conventionally known hydrotreating catalyst can be arbitrarily selected.
- a catalyst in which Ni, Mo, and Co sulfides are supported on alumina is preferable: Arabian.
- the pressure of hydrogen gas is, for example, 30 to 50 kg / cm.
- the sulfur concentration of the gas turbine fuel oil by setting 2 4 5 0 ppm or less, although the nitrogen concentration can be 3 0 ppm or less, which increases the pressure of the hydrogen gas to 4 0 ⁇ 7 ⁇ kg / cm 2 If the collision energy of hydrogen to the oil component molecules increases, the sulfur concentration and the nitrogen concentration can be suppressed to 200 ppm or less and 20 ppm or less, respectively.
- the residual oil (atmospheric pressure residual oil) 22 separated in the atmospheric pressure distillation column 2 is sent to the low pressure distillation column 5 where it is a light component of the atmospheric pressure residual oil, for example, having a boiling point of 5 6 at atmospheric pressure.
- Light oil lower than 5 C C (vacuum light oil) 51 and heavy oil (heavy oil whose atmospheric boiling point exceeds that) (vacuum residue) 52 are separated.
- the light oil 51 is sent to the second hydrotreating unit 6, where it is hydrotreated.
- the hydrogen gas used in the second hydrotreating device 6 is supplied from the hydrogen plant 4, and the gas having a low carbon number such as methane obtained in the second hydrotreating device 6 is supplied to the hydrogen plant 4. To be sent as production raw materials. Assuming that the pressure of hydrogen gas in the second hydrotreating unit 6 is 30 to 60 kg Z cm 2 , when the aforementioned Arabian light oil is used as a raw material, the sulfur concentration and the nitrogen concentration are respectively reduced. 2 0 0 0 pressure ppm hereinafter and 2 0 0 ppm force hydrogen gas can be below 5 0 to 1 0 0 kg / cm 2 Tosureba sulfur concentration and nitrogen concentration respectively 1 0 0 0 ppm or less And 100 ppm or lessc
- the light oil thus obtained in the second hydrotreating step is mixed with the light oil (gas turbine fuel oil) obtained in the first hydrotreating unit 3 (mixing step) and used as gas turbine fuel oil. I do.
- the heavy oil (vacuum residue) 52 separated in the vacuum distillation tower 5 is a solvent degreasing unit (solvent extraction unit) 7 1
- the degreasing oil 7 which is light oil in 7 1 and the degreasing oil which is heavy oil 7 This separation is carried out, for example, from the upper and lower parts of the column, respectively. And the solvent are supplied in countercurrent contact with each other, and light oil and heavy oil in the vacuum residual oil 52 are separated by a difference in solubility in the solvent.
- the separated deoiled oil 72 is mixed with the light oil 51 from the low-pressure distillation column 5 and supplied to the second hydrotreating unit 6.
- the residual residue oil 7 3 is used as a heavy oil feedstock or boiler fuel oil after its viscosity is adjusted as necessary.
- the processing performed in the first hydrogenation apparatus 3 and the processing performed in the second hydrogenation apparatus are
- the first and second hydrotreating steps correspond to the first and second hydrotreating steps, respectively.
- gas turbine fuel oil that satisfies the component rules described in the section of “Disclosure of the Invention” can be obtained. Since the hydrogenation process is performed after each of the atmospheric distillation process and the reduced pressure distillation process, each distillation process can be fired without worrying about the amount of sulfur and heavy metals.
- gas turbine fuel oil can be obtained in a high yield of at least 65%, preferably 70 to 90% (weight ratio) based on crude oil. it can.
- a heavy feedstock consisting of atmospheric distillation residue and Z or heavy oil is used as the starting feedstock, 40% or more, preferably 40 to 75% (weight Ratio) to obtain gas turbine fuel oil.
- distillation can be carried out at a ratio of light oil (60) and atmospheric residue (40).
- the pressure residue (40) can be distilled in the vacuum distillation tower 5 at a ratio of light oil (20) and vacuum residue (20).
- the reduced pressure residue (20) can be treated in the solvent degreasing device 71 at a ratio of deoiled oil (10) and desorbed residue (10).
- the gas turbine fuel oil will yield a total of 90% of light oil (60), reduced pressure light oil (20) and deoiled oil (10). If you do not perform the removal process Even at a yield of 80%.
- the gas turbine fuel oil has a yield of 65 ° / 0 or more, preferably 70 to 90%. You can get c
- the starting material is an atmospheric residual oil and a heavy feed oil (100) composed of Z or heavy oil
- the light oil (50) and the vacuum residue (50) The residue (50) can be further deoiled (25) and the residual oil (25) can be obtained in the solvent dewatering treatment device 71.
- the starting material for heavy feedstock is gas turbine fuel oil with a yield of 75% in total of decompressed light oil (50) and solvent degreasing oil (25). Gas turbine fuel oil can be obtained with a yield of 50%.
- FIG. 1 the case where heavy oil is desalted in the desalting section 12 and supplied to the vacuum distillation column 5 is indicated by a dotted line.
- heavy oil may be supplied to the vacuum distillation column 5 as shown by the dotted line in FIG. 1 or heavy oil may be supplied to the solvent dewatering device 71 (not shown).
- 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 amount of gas turbine fuel oil obtained based on crude oil has an effect on the yield for the feedstock oil.
- the amount of gas turbine fuel oil only increases in response to the additional feedstock (heavy oil), and this does not depart from the scope of the present invention.
- the light oil obtained in the second separation step that is, the deoiled oil 72 obtained in the solvent dewatering device 71 is limited to the treatment in the second hydrotreating device 6.
- the treatment may be performed by a separately provided third hydrotreating apparatus 60 (third hydrotreating step). If the second hydrotreating step and the third hydrotreating step are made common as in the embodiment of FIG. 1, the reaction conditions must be adjusted to the heavy oil side, so 5 0 ⁇ 1 5 0 kg Z cm 2, and the separate hydrogen pressure intends row becomes respectively for example 5 0 ⁇ 8 0 kg Z cm 2, 8 0 ⁇ 2 0 0 kg Z cm 2. If it is performed separately, the throughput in the third hydrotreating step, where the reaction conditions are severe, is small.Therefore, the advantage that the reaction vessel that can withstand high pressure can be miniaturized has the advantage If you adopt an advantageous configuration.
- the first and third hydrogenation steps may be a common step
- the first to third hydrotreating steps may be a common step.
- 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 a steam distillation method, a solvent stripping method, or a method using a residual oil 22 for example.
- a thermal cracking method of heating to 30 to 49 ° C. to cut hydrocarbon molecules by thermal energy to obtain light oil and heavy oil may be used.
- FIG. 6 is a view showing an embodiment in which the first separation step is carried out by a solvent stripping method. Atmospheric pressure residual oil 22 is supplied to a solvent stripping device 81, and is described in the previous embodiment.
- the light oil (solvent-removed oil) 82 and the light heavy oil (solvent-removed oil) 83 are the lightest oils among the atmospheric residual oils 22 and the light oil 82 is It is supplied to the hydrotreating unit 6 of 2.
- FIG. 7 is a diagram showing such an embodiment, in which the heavy oil (residual residue oil) 83 separated by the solvent degreasing device 81 is transferred to the fourth hydrotreating device 91. It is supplied and separated into light oil 92 and heavy oil 93.
- the fourth hydrotreating device 91 is provided at the subsequent stage of the device shown in FIG.
- the gas turbine fuel oil is obtained also from the heavy oil separated in the first separation step (in this example, the solvent removal step) including the vacuum distillation apparatus. Therefore, there is an advantage that the recovery rate of gas turbine fuel oil from the feedstock oil is higher.In addition, a part of the feedstock oil is mixed with the heavy oil 83 It may be supplied to the hydrotreating device 91 of 4.
- the residual oil 22 separated in the atmospheric distillation step is supplied to a fifth hydrotreating apparatus 101, where the fifth oil is treated. Is separated into light oil 102 and heavy oil 103 by mixing the light oil 102 with the gas turbine fuel oil obtained in the first hydrotreating unit 3. You can use it.
- the fifth hydrotreating device 101 also includes a distillation device as in the fourth hydrotreating device 91.
- the heavy oil 103 is supplied to the solvent degreasing device 111, where it is separated into light oil (degreasing oil) 112 and heavy oil (drag residue) 113.
- the separated light oil 1 1 2 is used as a gas turbine fuel oil, for example, by mixing with the light oil 1 0 2 obtained in the fifth hydrotreating unit 101, and the heavy oil 1 13 Used as boiler fuel.
- the third separation step is not limited to the solvent removal step, and may be the above-described thermal decomposition step or reduced-pressure distillation step. Even in such an embodiment, the recovery rate of the gas turbine fuel oil from the feed oil can be 65 ° / 0 or more, preferably 70 to 90%.
- the fourth or fifth hydrotreating unit 91 (101) described in Figs. 7 and 8 light oil (gas) such as methane produced here is also treated with hydrogen plan. Sent to 4 and used as a raw material for producing hydrogen gas.
- the reaction conditions for hydrotreating are set according to the heavy oil in the feedstock.
- the heavy oil corresponds to light oil (vacuum light oil) 51.
- vacuum distillation is taken as an example of the first separation step, but the invention is not limited to this, and the light oil obtained in the first separation step by another process and the light oil 21 may be used.
- the hydroprocessing unit 61 may perform batch processing.
- sulfur pressure of hydrogen gas for example 3 0 ⁇ 6 0 kg / cm 2 by Ri gas turbine fuel oil to be set concentration 5 0 0 ppm or less, although the nitrogen concentration can be under 5 0 ppm or less, 0 5 0-1 0 the pressure of the hydrogen gas kg Z cm 2 to raise that if the sulfur concentration and nitrogen concentration respectively 3 It can be suppressed to below 0 ppm and below 30 ppm.
- the refined oil obtained by batch processing in the hydrotreating unit 61 as described above can be used as a + partition gas turbine fuel oil, but as shown in FIG. Is distilled in an atmospheric distillation column 62 at, for example, 350 ° C., and the obtained light oil is purified to a high quality.
- High quality (light) gas turbine fuel oil and residual oil may be used as heavier gas turbine fuel oil than its higher quality c
- the heavy oil obtained in the above-described first separation step, second separation step and Z or the third separation step is partially oxidized with oxygen gas to generate hydrogen, and the hydrogen is converted to hydrogen. It may be used in a chemical treatment device.
- This hydrotreating apparatus may be a hydrotreating apparatus used in the first to fourth hydrotreating steps.
- FIG. 11 shows an example of such a method, in which the residual oil from the solvent dewatering device 81 is partially oxidized, and the hydrogen obtained here is converted into the first hydrotreating device 3 and the second hydrogen. The case where it supplies to the chemical treatment apparatus 6 is shown.
- 63 is an oxygen plant that extracts oxygen from air
- 64 is a partial oxidation unit.
- the heavy oil to be partially oxidized is not limited to the solvent desorption device 81, but may be the residual oil obtained in the first separation step in another process such as the distillation column 5, or the second oil.
- the heavy oil obtained in the third separation step may be used.
- FIG. 12 is a diagram schematically showing an example of the partially oxidized rice paddy 64.
- heavy oil and high-pressure steam are pre-heated and injected together with oxygen into a reaction furnace 65, for example, at a temperature of 1200 to 150 ° C. and 2 to 85 kg Z cm 2 .
- a gas consisting mainly of CO and H2 is generated by a partial oxidation reaction under process conditions.
- This gas is then quenched with water, for example, to 200-26 (TC) in a quench chamber at the bottom of the reactor 65, where most of the unreacted carbon is removed and
- the required steam is supplied to the gas, which is sent to a washing tower 66 to completely remove the small amount of unreacted carbon, and further sent to a CO converter 67 to, for example, cobalt by reaction with steam residual CO by Ribuden based catalyst converted into C_ ⁇ 2.
- 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.
- Gas turbine fuel oil is burned by a combustion nozzle and The gas turbine 201 is driven by the combustion gas, and electric power is extracted from the generator 202.
- the high-temperature exhaust gas discharged from the gas turbine 201 is supplied to an exhaust heat recovery boiler 203 to generate steam by the heat of the exhaust gas.
- the steam drives the steam turbine 204 by this steam, and power is extracted from the generator 205. If power is generated in this way, the exhaust heat of gas turbine fuel oil can be effectively used, and power generation can be performed with high efficiency.
- Gas turbine fuel oil was manufactured using the system shown in Fig. 1 using Arabian light crude oil (S content: 1.77 weight./.), Which is the easiest to procure in the market.
- S content 1.77 weight./.
- the atmospheric distillation step light oil 21 having a boiling point lower than 350 ° C and heavy oil 22 having a higher boiling point are separated into two, and the pressure of hydrogen gas in the first hydrotreating step is raised to 45 5
- the gas turbine fuel oil was obtained at a setting of kg Z cm 2 .
- a gas turbine fuel oil was produced by using Arabian light oil as a crude oil according to the description in Japanese Patent Application Laid-Open No. 6-207179-a low-sulfur crude oil in which the salt concentration was adjusted to 0.5 ppm or less. Is used to produce gas turbine fuel oil of 0.05 wt ° / 0 or less.
- Arabian's light oil has a high sulfur content to be defined as a low-sulfur crude oil, but is currently the most stable crude oil available on the market. Based on the above, a petroleum fraction having a sulfur concentration of 0.05 wt% or less was separated by a distillation method.
- Gas turbine fuel oil from this gazette technology is limited to light naphtha to kerosene fractions in the boiling range up to 245 ° C. Alkali metals, alkaline earth metals, V and lead are not detected, and sulfur concentration was about 470 ppm and the viscosity was 0.3 cSt at 100 ° C, but the recovery rate of gas turbine fuel oil to feedstock was 24%, which was extremely low recovery.
- Alkali metals, alkaline earth metals, V and lead are not detected, and sulfur concentration was about 470 ppm and the viscosity was 0.3 cSt at 100 ° C, but the recovery rate of gas turbine fuel oil to feedstock was 24%, which was extremely low recovery.
- Example 2 The simulation was performed under the same conditions as in Example 1 except that the in-house consumption rate of the refined blunt was 3%.
- the supply of crude oil to the refinery plant was 100 units in terms of calories, and the final amount of power recovery was calculated, only 39.5 units of power energy could be recovered in terms of calories. It turned out to be significantly inferior in terms of use.
- Oman crude oil which is a relatively low-sulfur crude oil in the Middle East, was used to produce gas turbine fuel oil.
- Oman crude oil has a sulfur concentration of 0.94 wt% and corresponds to the low sulfur crude oil described in Japanese Patent Application Laid-Open No. 6-207179.
- light oil 21 with a boiling point lower than 350 ° C and heavy oil 22 with a higher boiling point are separated into two, and the pressure of hydrogen gas in the first hydrotreating step is reduced to 4
- a gas turbine fuel oil was obtained at a setting of 0 kg / cm 2 .
- the boiling point is 51, which is light oil whose boiling point (boiling point at normal pressure) is lower than 565 ° C.
- the pressure of the hydrogen gas in the second hydrotreating is set to 5 0 kg Z cm 2 to obtain a gas turbine fuel oil
- the first hydrotreating It was mixed with the obtained gas turbine fuel oil.
- gas turbine fuel oil, no alkali metal, alkaline earth metal, V and lead were detected, the sulfur concentration was approximately 410 ppm, and the viscosity was 1.0 at 100 ° C. 1 c St.
- the yield of gas turbine fuel oil based on the feed oil was 85%. This gas turbine fuel oil could be used in a gas turbine with a gas turbine inlet temperature of 130 ° C.
- the simulation was performed on the assumption that all energy from crude oil would be converted to electric power (gas turbine and boiler power generation).
- the on-site consumption rate at the refining plant was set at 4%, and the combined cycle gas turbine power generation efficiency was set at 49% and the boiler power generation efficiency at 38%.
- the supply of crude oil to the refinery plant was set at 100 units in terms of calories, and the final amount of power recovery was calculated. As a result, 45.8 units of power energy could be recovered in terms of calories.
- a gas turbine fuel oil was produced using Oman crude oil as an example in the same manner as in Example 2 according to the technique disclosed in JP-A-6-207179.
- the production method was the same as in Comparative Example 1, and a petroleum fraction having a sulfur concentration of 0.05 wt% or less was separated from the crude oil by a distillation method based on JP-A-6-207179.
- Gas turbine fuel oil from this publication is limited to light naphtha to kerosene fractions in the boiling point range up to 250 ° C. Alkaline metals, alkaline earth metals, V and lead are not detected, and sulfur concentration Was approximately 49 ppm and the viscosity was 0.45 cSt at 100 ° C.
- the yield of distillate separated gas turbine fuel oil was as high as 35%. Low recovery.
- Example 2 The simulation was performed under the same conditions as in Example 2 except that the in-house consumption rate in the refined blunt was 3%.
- the crude oil supply to the refining plant was calculated as 100 units in terms of calories, and the final amount of power recovery was calculated.As a result, only 40.7 units of power energy could be recovered in terms of calories, and it was a low-sulfur crude oil. Even compared to the present invention It turned out to be significantly inferior in terms of effective energy use c
- crude oil is subjected to normal pressure distillation, the light oil is subjected to hydrogenation treatment, and the normal pressure residue is subjected to separation treatment or hydrogenation treatment. Since the oil is hydrotreated and the refined oil is used as gas turbine fuel oil, high quality gas turbine fuel oil can be obtained in high yield.
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US09/807,696 US7276151B1 (en) | 1998-10-30 | 1999-09-10 | Gas turbine fuel oil and production method thereof and power generation method |
EP99943259A EP1130080A4 (en) | 1998-10-30 | 1999-09-10 | FUEL OIL FOR GAS TURBINES AND METHOD FOR THE PRODUCTION AND PRODUCTION OF ELECTRICITY |
BR9914885-4A BR9914885A (pt) | 1998-10-30 | 1999-09-10 | Processo para produção de óleo combustìvel para turbina de gás e processo para geração de energia |
Applications Claiming Priority (6)
Application Number | Priority Date | Filing Date | Title |
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JP32616998 | 1998-10-30 | ||
JP10/326169 | 1998-10-30 | ||
JP11/10847 | 1999-01-19 | ||
JP1084799 | 1999-01-19 | ||
JP08943399A JP5057315B2 (ja) | 1998-10-30 | 1999-03-30 | ガスタービン燃料油の製造方法 |
JP11/89433 | 1999-03-30 |
Publications (1)
Publication Number | Publication Date |
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WO2000026325A1 true WO2000026325A1 (fr) | 2000-05-11 |
Family
ID=27279120
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP1999/004927 WO2000026325A1 (fr) | 1998-10-30 | 1999-09-10 | Huile combustible pour turbine a gaz, son procede de production et procede de production d'energie |
Country Status (12)
Country | Link |
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US (1) | US7276151B1 (ja) |
EP (1) | EP1130080A4 (ja) |
JP (1) | JP5057315B2 (ja) |
KR (1) | KR100432293B1 (ja) |
AR (1) | AR021040A1 (ja) |
BR (1) | BR9914885A (ja) |
ID (1) | ID29869A (ja) |
RU (1) | RU2203926C2 (ja) |
SA (1) | SA99200527B1 (ja) |
TR (1) | TR200101172T2 (ja) |
TW (1) | TW467951B (ja) |
WO (1) | WO2000026325A1 (ja) |
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- 1999-03-30 JP JP08943399A patent/JP5057315B2/ja not_active Expired - Fee Related
- 1999-08-25 SA SA99200527A patent/SA99200527B1/ar unknown
- 1999-09-10 BR BR9914885-4A patent/BR9914885A/pt not_active Application Discontinuation
- 1999-09-10 US US09/807,696 patent/US7276151B1/en not_active Expired - Fee Related
- 1999-09-10 WO PCT/JP1999/004927 patent/WO2000026325A1/ja active IP Right Grant
- 1999-09-10 EP EP99943259A patent/EP1130080A4/en not_active Withdrawn
- 1999-09-10 TR TR2001/01172T patent/TR200101172T2/xx unknown
- 1999-09-10 ID IDW00200101164A patent/ID29869A/id unknown
- 1999-09-10 RU RU2001114512/04A patent/RU2203926C2/ru not_active IP Right Cessation
- 1999-09-10 KR KR10-2001-7005384A patent/KR100432293B1/ko not_active IP Right Cessation
- 1999-10-28 TW TW088118689A patent/TW467951B/zh not_active IP Right Cessation
- 1999-10-29 AR ARP990105499A patent/AR021040A1/es active IP Right Grant
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Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2001036566A1 (en) * | 1999-11-15 | 2001-05-25 | Jgc Corporation | System and method for oil fuel burning integrated combined cycle power generation |
EP1350832A4 (en) * | 2000-11-30 | 2004-12-01 | Jgc Corp | METHOD FOR REFINING PETROLEUM |
US7846912B2 (en) | 2007-09-13 | 2010-12-07 | Protia, Llc | Deuterium-enriched nelarabine |
US8850787B2 (en) | 2010-05-27 | 2014-10-07 | Sumitomo Corporation | Hybrid thermal power generation system and method of constructing same |
Also Published As
Publication number | Publication date |
---|---|
KR20010089377A (ko) | 2001-10-06 |
TW467951B (en) | 2001-12-11 |
KR100432293B1 (ko) | 2004-05-22 |
SA99200527B1 (ar) | 2006-08-12 |
EP1130080A4 (en) | 2004-11-24 |
US7276151B1 (en) | 2007-10-02 |
TR200101172T2 (tr) | 2001-09-21 |
BR9914885A (pt) | 2002-01-15 |
EP1130080A1 (en) | 2001-09-05 |
ID29869A (id) | 2001-10-18 |
AR021040A1 (es) | 2002-06-12 |
RU2203926C2 (ru) | 2003-05-10 |
JP2000273467A (ja) | 2000-10-03 |
JP5057315B2 (ja) | 2012-10-24 |
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