Information processing method, hydrogen consumption calculation device, hydrogen consumption calculation program, and non-transitory computer-readable recording medium

Abstract

To provide, regarding hydrotreating reaction of raw oil including gas oil fraction, an information processing method capable of estimating a hydrogen consumption, a hydrogen consumption calculation device capable of estimating the hydrogen consumption, a hydrogen consumption calculation program, and a non-temporary readable recording medium for a computer.SOLUTION: An information processing method, regarding hydrotreating reaction of raw oil including gas oil fraction, includes: an information acquisition step to acquire information on raw oil in a fixed period, and information on product oil; and a hydrogen quantity calculation step to calculate a hydrogen quantity consumed by the hydrotreating reaction in fixed period on the basis of the acquired information on raw oil, and the acquired information on product oil.SELECTED DRAWING: None

Description

[Technical Field]

[0001] The present invention relates to an information processing method, a hydrogen consumption calculation device, a hydrogen consumption calculation program, and a non-transitory computer-readable recording medium. [Background technology]

[0002] Diesel oils used as fuel for diesel engines and the like are produced by hydrotreating straight-run diesel oil fractions of a specific boiling point range obtained by atmospheric distillation of crude oil, or cracked diesel oil fractions obtained by cracking heavy oil, or by blending a hydrotreated diesel oil fraction with an unhydrotreated diesel oil fraction. Hydrotreating a diesel oil fraction reduces the sulfur content of the diesel oil fraction and also improves its properties as a fuel for diesel engines, such as color and cetane number.

[0003] In the hydrotreating of feedstock containing diesel fractions, operational constraints such as reaction temperature and hydrogen consumption are set. Regarding reaction temperature, a maximum operating temperature is set for a hydrotreating unit depending on its material, structure, and the capacity of its peripheral equipment, and the unit must be operated at or below this maximum operating temperature. Regarding hydrogen consumption, depending on the hydrogen supply environment of the refinery, a shortage of hydrogen can limit the throughput of feedstock containing diesel fractions. Therefore, a method for accurately estimating reaction temperature and hydrogen consumption is needed.

[0004] Patent Document 1 discloses a method for estimating the reaction temperature required after switching between straight-run diesel fractions with different properties as feedstock in the hydrotreatment of straight-run diesel fractions, based on information on the properties of the straight-run diesel fraction before switching and the operating conditions, and information on the properties of the straight-run diesel fraction after switching and the operating conditions other than the reaction temperature. [Prior art documents] [Patent documents]

[0005] [Patent Document 1] Japanese Patent Application Publication No. 10-60455 Summary of the Invention [Problem to be solved by the invention]

[0006] In the hydrotreating method of straight-run diesel oil fraction described in Patent Document 1, hydrogen consumption is not considered, and a value calculated based on actual results is used as the hydrogen consumption. As mentioned above, hydrogen consumption can be an operational constraint. Furthermore, since hydrogen consumption has a large impact on the cost of hydrotreating, a method for accurately estimating hydrogen consumption is desired.

[0007] The present invention has been made in consideration of the above circumstances, and aims to provide an information processing method capable of estimating hydrogen consumption in a hydrotreating reaction of feedstock oil containing a light oil fraction, a hydrogen consumption calculation device capable of estimating the hydrogen consumption, a hydrogen consumption calculation program, and a non-transitory computer-readable recording medium. [Means for solving the problem]

[0008] In order to solve the above problems, the present invention has the following aspects. [1] An information processing method for a hydrotreating reaction of a feedstock containing a light oil fraction, comprising: an information acquisition step of acquiring information about the feedstock and information about the product oil for a certain period of time; and a hydrogen amount calculation step of calculating the amount of hydrogen consumed in the hydrotreating reaction for the certain period of time based on the acquired information about the feedstock and information about the product oil. [2] The information processing method according to [1], wherein the hydrotreating reaction includes a hydrodesulfurization reaction, a hydrocracking reaction, and a hydrogenation reaction, and the hydrogen amount calculation step is a step of calculating the amount of hydrogen consumed in the hydrodesulfurization reaction, the hydrocracking reaction, and the hydrogenation reaction during the certain period. [3] The information processing method described in [1] or [2], wherein the information regarding the feedstock oil includes information regarding the composition of the feedstock oil and the supply amount of the feedstock oil, and the information regarding the produced oil includes information regarding the composition of the produced oil. [4] The information processing method according to [3], wherein the information on the composition of the feedstock oil includes information on the sulfur concentration in the feedstock oil, information on the naphtha concentration in the feedstock oil, and information on the aromatic compound concentration in the feedstock oil, and the information on the composition of the produced oil includes information on the sulfur concentration in the produced oil, information on the naphtha concentration in the produced oil, and information on the aromatic compound concentration in the produced oil. [5] The information processing method according to [3] or [4], wherein the information relating to the feedstock oil includes information relating to the density of the feedstock oil, and the information relating to the produced oil includes information relating to the density of the produced oil. [6] A hydrogen consumption calculation device comprising: an acquisition unit that acquires information about a feedstock oil and information about a product oil over a certain period of time in relation to a hydrotreating reaction of a feedstock oil containing a light oil fraction; and a calculation unit that calculates the amount of hydrogen consumed in the hydrotreating reaction over the certain period of time based on the information about the feedstock oil and the information about the product oil acquired by the acquisition unit. [7] The hydrogen consumption calculation device according to [6], wherein the hydrotreating reaction includes a hydrodesulfurization reaction, a hydrocracking reaction, and a hydrogenation reaction, and the calculation unit calculates the amount of hydrogen consumed in the hydrodesulfurization reaction, the hydrocracking reaction, and the hydrogenation reaction during the certain period. [8] The hydrogen consumption calculation device described in [6] or [7], wherein the information about the feedstock oil includes information about the composition of the feedstock oil and information about the supply amount of the feedstock oil, and the information about the product oil includes information about the composition of the product oil. [9] The hydrogen consumption calculation device according to [8], wherein the information on the composition of the feedstock oil includes information on the sulfur concentration in the feedstock oil, information on the naphtha concentration in the feedstock oil, and information on the aromatic compound concentration in the feedstock oil, and the information on the composition of the produced oil includes information on the sulfur concentration in the produced oil, information on the naphtha concentration in the produced oil, and information on the aromatic compound concentration in the produced oil.

[10] The hydrogen consumption calculation device according to [8] or [9], wherein the information relating to the feedstock oil includes information relating to the density of the feedstock oil, and the information relating to the product oil includes information relating to the density of the product oil.

[11] A hydrogen consumption calculation program for causing a computer to function as the hydrogen consumption calculation device according to any one of [6] to

[10] .

[12] A non-transitory computer-readable recording medium storing the program described in

[11] . [Effects of the Invention]

[0009] According to the present invention, it is possible to provide an information processing method capable of estimating hydrogen consumption in a hydrotreating reaction of a feedstock oil containing a light oil fraction, a hydrogen consumption calculation device capable of estimating the hydrogen consumption, a hydrogen consumption calculation program, and a non-transitory computer-readable recording medium. [Brief explanation of the drawings]

[0010] [Figure 1] 1 is a flowchart of an information processing method according to an embodiment. [Figure 2] 1 is a flowchart of an information processing method according to an embodiment. [Figure 3] 1 is a configuration block diagram of a hydrogen consumption amount calculation device according to an embodiment. [Figure 4] FIG. 1 is a configuration block diagram of a naphtha yield calculation device according to an embodiment. DETAILED DESCRIPTION OF THE INVENTION

[0011] The following describes in detail the embodiments of the present invention. However, the following description is an example of an embodiment of the present invention, and the present invention is not limited to these contents and can be modified and implemented within the scope of its gist.

[0012] <Information processing method> The information processing method of this embodiment includes an information acquisition step (S1 in FIG. 1) of acquiring information about the feedstock and information about the product oil for a certain period of time regarding the hydrotreating reaction of the feedstock containing a diesel fraction, and a hydrogen amount calculation step (S2 in FIG. 1) of calculating the amount of hydrogen consumed in the hydrotreating reaction for the certain period of time based on the acquired information about the feedstock and information about the product oil. Each step will be explained below. Note that each step shown below is executed, for example, by the hydrogen consumption calculation device 1 of this embodiment. For example, S1 is executed by the acquisition unit 11, and S2 is executed by the calculation unit 13 in the computer main body 12.

[0013] <Information Acquisition Steps> The information acquisition step of this embodiment is a step of acquiring information about feedstock oil and information about product oil for a certain period of time. The information acquisition step may acquire information about operating conditions for a certain period of time. The certain period is, for example, s days. s may be an integer or a decimal; for example, s = 0.5 means 12 hours. s can be determined appropriately depending on the operating conditions, etc., and may be 0.1 to 1000, or 0.1 to 50. Furthermore, the certain period may be a past period from the time when the information processing method of this embodiment is performed, a period including the present, or a future period. For example, if the information acquired in the information acquisition step is a measured value, the period may be a past period or a period including the present from the time when the information processing method is performed. On the other hand, if the information acquired in the information acquisition step is a set value or an estimated value, the period may be a future period.

[0014] (Information about raw material oil) Examples of the information about the feedstock include information about the composition of the feedstock, information about the density of the feedstock, and information about the feedstock supply amount. Examples of the information about the composition of the feedstock include information about the naphtha concentration in the feedstock, information about the aromatic compound concentration in the feedstock, and information about the sulfur concentration in the feedstock.

[0015] Information regarding the sulfur concentration in the feedstock oil can be obtained by methods for measuring sulfur concentration known in the art, such as ultraviolet fluorescence spectroscopy and wavelength dispersive X-ray fluorescence spectroscopy. Information regarding the naphtha concentration in the feedstock oil can be obtained by a method for measuring naphtha concentration known in the art, such as calculation from the proportion of fractions at 175°C or less in a distillation test such as ASTM D-6730. Information regarding the concentration of aromatic compounds in the feedstock oil can be obtained by methods for measuring the concentration of aromatic compounds known in the art, such as high performance liquid chromatography (HPLC) and gas chromatography gravimetric analysis (GC-MS measurement).

[0016] Information about the density of the feedstock oil can be obtained by density measurement methods known in the art. For example, the density of the feedstock oil can be obtained by correcting the 15°C density obtained according to JIS K2249 "Crude oil and petroleum products - Density test method and density, mass, and volume conversion table" by temperature.

[0017] The information about the feed rate can be obtained by a method for measuring the feed rate of the feed oil known in the art, such as a flow meter. The information about the feed rate can be controlled. That is, the information about the feed rate of the feed oil is preferably a set value.

[0018] (Information about the produced oil) Examples of the information about the product oil include information about the composition of the product oil and information about the density of the product oil. Examples of the information about the composition of the product oil include information about the naphtha concentration in the product oil, information about the aromatic compound concentration in the product oil, and information about the sulfur concentration in the product oil.

[0019] Information about the sulfur concentration in the produced oil, information about the naphtha concentration in the produced oil, and information about aromatic compounds in the produced oil can be obtained in the same manner as in the case of the feed oil described above. Information about the density of the produced oil can be obtained in the same manner as in the case of the feed oil described above.

[0020] In the above, methods for measuring information on the sulfur concentration in the feed oil and the product oil, information on the concentration of naphtha, information on aromatic compounds, and information on the densities of the feed oil and the product oil have been explained, but if these values ​​are known or there are assumed values ​​for operation, these values ​​can also be used.

[0021] The information on the feedstock oil and the information on the product oil for a certain period of time may be acquired only once or multiple times during the certain period of time. If the information is acquired multiple times, the average value of the information on the feedstock oil and the information on the product oil for the certain period of time may be used.

[0022] (Information about operating conditions) Examples of information about operating conditions include information about hydrogen partial pressure, information about catalyst loading, and information about the amount of hydrogen supplied. For example, the information about operating conditions is at least one of information about hydrogen partial pressure, information about catalyst loading, and information about the amount of hydrogen supplied. Among these, it is more preferable to include all of information about hydrogen partial pressure, information about catalyst loading, and information about the amount of hydrogen supplied. In addition, the operating conditions also include information about time, such as a certain period of s days after the start of the reaction or an arbitrary number of t days.

[0023] The information on the hydrogen partial pressure, the catalyst loading amount, and the hydrogen supply amount can be determined by methods known in the art. The information on the hydrogen partial pressure, the catalyst loading amount, and the hydrogen supply amount can be controlled in the hydrotreating reaction of feedstock oil containing a light oil fraction. The information on the operating conditions is preferably a set value. That is, the planned operating conditions are used.

[0024] The information on the operating conditions for a certain period may be acquired only once during the certain period, or may be acquired multiple times. If the information is acquired multiple times, the average value thereof may be used as the information on the operating conditions for the certain period.

[0025] <Hydrogen amount calculation step> The hydrogen amount calculation step of this embodiment is a step of calculating the amount of hydrogen consumed in the hydrotreating reaction over a certain period of time based on the information about the feedstock oil and the information about the product oil acquired in the information acquisition step. In this embodiment, it is preferable to calculate the amount of hydrogen using a hydrogen consumption calculation function described below.

[0026] The inventors of the present application have discovered that by calculating the difference between a specific component contained in the feedstock oil and the same specific component contained in the refined oil, it is possible to focus on the hydrogen consumption resulting from the difference in components and accurately calculate the actual hydrogen consumption.

[0027] The hydrogen consumption calculation function of this embodiment is preferably a function that calculates the sum of the amount of hydrogen consumed by the hydrodesulfurization reaction, the amount of hydrogen consumed by the hydrocracking reaction, and the amount of hydrogen consumed by the hydrogenation reaction. An example of such a hydrogen consumption calculation function is the hydrogen consumption function expressed by the following equation 1.

[0028]

number

[0029] H CThe unit of is not particularly limited as long as it is a unit that expresses the amount of hydrogen, and for example, volume, mol, etc. can be used. F(ave) and S P(ave) The unit of is not particularly limited as long as it is a unit that expresses concentration, and for example, mass %, volume %, etc. can be used. However, S F(ave) and S P(ave) The units are the same. P(ave) and NA F(ave) The unit of NA is not particularly limited as long as it is a unit that expresses concentration, and for example, mass % or volume % can be used. P(ave) and NA F(ave) The units are the same. F(ave) and AR P(ave) The unit of AR is not particularly limited as long as it is a unit that expresses concentration, and for example, mass % or volume % can be used. F(ave) and AR P(ave) The unit of L is not particularly limited as long as it is a unit that represents the amount of feedstock oil supplied, and for example, volume, mass, mol, etc. can be used. In the formula 1, S F(ave) and S P(ave) Units of NA P(ave) and NA F(ave) Units of AR and F(ave) and AR P(ave) The units may be the same or different. In this embodiment, for example, H C The unit is [Nm 3 ], S F(ave) and S P(ave) The unit is [mass%], NA P(ave) and N.A. F(ave) The unit is [volume %], AR F(ave) and AR P(ave) The unit of can be [volume %] and the unit of L can be [kL].

[0030] In the formula 1, (S F(ave) -S P(ave) ) is a term that quantitatively indicates the extent to which the hydrodesulfurization reaction has progressed over a certain period of time, and a1(S F(ave) -S P(ave) ) is a term that estimates the amount of hydrogen consumed by the hydrodesulfurization reaction. (NAP(ave) -NA F(ave) ) is a term that indicates the extent to which the hydrocracking reaction that produces naphtha has progressed over a certain period of time, and a2(NA P(ave) -NA F(ave) ) is a term that estimates the amount of hydrogen consumed by the hydrocracking reaction that produces naphtha. (AR F(ave) -AR P(ave) ) is a term that indicates how much the hydrogenation reaction has progressed in a certain period of time, and a3(AR F(ave) -AR P(ave) ) is a term that estimates the amount of hydrogen consumed by the hydrogenation reaction.

[0031] (How to set tuning factors a1, a2, a3) Tuning factor a1 is a tuning factor for converting the progress of the hydrodesulfurization reaction that has proceeded over a certain period of time into the amount of hydrogen consumed by the reaction. Tuning factor a2 is a tuning factor for converting the progress of the naphtha-producing hydrocracking reaction that has proceeded over a certain period of time into the amount of hydrogen consumed by the reaction. Tuning factor a3 is a tuning factor for converting the progress of the hydrogenation reaction that has proceeded over a certain period of time into the amount of hydrogen consumed by the reaction.

[0032] The method for obtaining the tuning factors a1, a2, and a3 is not particularly limited, but they can be obtained by comparing with the actual measured value of the amount of hydrogen consumed over a certain period. An example will be explained below. By using the above method, S F(ave) , S P(ave) , N.A. P(ave) , N.A. F(ave) , A.R. F(ave) , A.R. P(ave) , L information is acquired, and the estimated hydrogen consumption H C In this case, H C is a function of a1, a2, and a3. RC =H C We can obtain a1, a2, and a3 such that

[0033] The actual hydrogen consumption over a certain period of time, H RC can be obtained by a method for measuring hydrogen consumption known in the art. In an actual system, the following measurement method can be cited as an example. In an actual system, a fixed amount of hydrogen is supplied to the reactor (supplied hydrogen), and unreacted hydrogen discharged from the reactor outlet (recycled hydrogen) is used as part of this supplied hydrogen. On the other hand, the amount of recycled hydrogen is less than the amount of supplied hydrogen. By separately supplying an amount of hydrogen equivalent to this shortage (make-up hydrogen), the amount of supplied hydrogen becomes constant. The amount of this make-up hydrogen is the actual measured value of hydrogen consumption. Make-up hydrogen can be measured using a flow meter.

[0034] On a bench scale, the amount of hydrogen consumed can be calculated, for example, by the following formula 2.

[0035]

number

[0036] H H2S is the above (S F(ave) -S P(ave) ) to calculate the difference in sulfur concentration over a certain period of time, convert the resulting difference into H2S, and calculate the amount of hydrogen converted from the amount of H2S. H NH3The difference between the nitrogen concentration in the feedstock oil and the nitrogen concentration in the produced oil over a certain period is calculated, and the obtained difference is converted into NH3, which can then be calculated as the amount of hydrogen converted from the amount of NH3. H HC can be calculated as hydrogen converted from the amount of hydrocarbons with carbon numbers of 1 to 6 obtained by analyzing the reactor outlet gas for a certain period by gas chromatography. H P is the amount of hydrogen obtained by CHN macroanalysis of the oil produced over the given period. H SOL is the amount of hydrogen calculated from the amount of dissolved hydrogen based on Henry's law. H F is the amount of hydrogen obtained by CHN macroanalysis of the feedstock oil for the specified period. Here, regardless of the reaction period, H SOL can be set to a constant value, so from the above equation 2, H SOL may be excluded.

[0037] To obtain a more accurate estimated hydrogen consumption, the actual hydrogen consumption values ​​H RC and the estimated hydrogen consumption H C It is preferable to compare the actual measured value of hydrogen consumption for a certain period with H RC (n), and the estimated hydrogen consumption is H C (n), where n represents the number of measured periods and is an integer equal to or greater than 2. For all n, H RC (n) / H C It is preferable to obtain a1, a2, and a3 such that (n) is 0.9 to 1.1. n is preferably 10 or more, and more preferably 20 or more. The certain period is not particularly limited, but may be, for example, 10 to 300 days. The tuning factors a1, a2, and a3 may be obtained while carrying out the hydrotreating reaction in an actual machine, or may be obtained in advance on a bench scale.

[0038] The hydrogen consumption amount calculation function may be the hydrogen consumption function expressed by the following equation 3.

[0039]

number

[0040] The inventors of the present application calculated the difference between the average density of the feedstock oil and the average density of the product oil over a certain period of time to determine the progress of the hydrogenation reaction (AR F(ave) -AR P(ave) ) was found to be a possible substitute. That is, (DE F(ave) -DE P(ave) ) is a term indicating how much the hydrogenation reaction has progressed during the given period, and b3(DE F(ave) -DE P(ave) ) is a term for estimating the amount of hydrogen consumed by the hydrogenation reaction. According to the above formula 3, it is not necessary to obtain information about the concentration of aromatic compounds in the feed oil and the concentration of aromatic compounds in the product oil, and it is possible to more simply calculate the estimated hydrogen consumption amount H C can be obtained.

[0041] (How to set tuning factors b1, b2, and b3) Tuning factor b1 is a tuning factor for converting the progress of the hydrodesulfurization reaction that has proceeded over a certain period of time into the amount of hydrogen consumed by the reaction. Tuning factor b2 is a tuning factor for converting the progress of the naphtha-producing hydrocracking reaction that has proceeded over a certain period of time into the amount of hydrogen consumed by the reaction. Tuning factor b3 is a tuning factor for converting the progress of the hydrogenation reaction that has proceeded over a certain period of time into the amount of hydrogen consumed by the reaction.

[0042] The method for obtaining tuning factors b1, b2, and b3 is not particularly limited, but they can be obtained by comparing with the actual measured value of hydrogen consumption over a certain period, similar to the method for obtaining tuning factors a1, a2, and a3 described above. An example is described below. By using the above method, S F(ave) , S P(ave) , N.A. P(ave) , N.A. F(ave) , D.E. F(ave) , D.E. P(ave) , L information is acquired, and the estimated hydrogen consumption amount H C In this case, H C is a function of b1, b2, and b3. RC =H C We can obtain b1, b2, and b3 such that

[0043] To obtain a more accurate estimated hydrogen consumption, the actual hydrogen consumption values ​​H RC and the estimated hydrogen consumption H C It is preferable to compare the actual measured value of hydrogen consumption for a certain period with H RC (n), and the estimated hydrogen consumption is H C (n), where n represents the number of measured periods and is an integer equal to or greater than 2. For all n, H RC (n) / H C It is preferable to obtain b1, b2, and b3 such that (n) is 0.9 to 1.1. n is preferably 10 or more, more preferably 20 or more. The certain period is not particularly limited, but may be, for example, 10 to 300 days. The tuning factors b1, b2, and b3 may be obtained while carrying out the hydrotreating reaction in an actual machine, or may be obtained in advance on a bench scale.

[0044] The hydrogen consumption amount calculation function may be the hydrogen consumption function expressed by the following equation 4.

[0045]

number

[0046]

number

[0047] The inventors of the present application have found that, once the catalyst to be used is determined, the estimated average density of the product oil can be obtained from the average reaction temperature over a certain period and the average density of the feedstock oil. That is, (DE F(ave) -DE P(ave) ’ ) is a term that indicates how much the hydrogenation reaction has progressed in a certain period of time, and b3(DE F(ave) -DE P(ave) ’ )f H is a term for estimating the amount of hydrogen consumed by the hydrogenation reaction. According to Equation 4, it is not necessary to obtain information about aromatic compounds in the feed oil, information about aromatic compounds in the product oil, and information about the density of the product oil, and it is therefore possible to more simply obtain the estimated hydrogen consumption amount for the certain period.

[0048] (Method of setting catalyst coefficients α, β, σ) The catalyst coefficients α, β, and σ are coefficients determined for each catalyst for calculating the estimated average density of the product oil over a certain period from the average density of the feedstock oil over that period and the average reaction temperature over that period.

[0049] The method for obtaining the catalyst coefficients α, β, and σ is not particularly limited, but they can be obtained by comparing with the actual measured value of the average density of the produced oil for a certain period. An example will be described below. DE for a certain period using the above method F(ave) , D.E. P(ave) and T information is obtained, and DE is calculated using Equation 5. P(ave) In this case, DE P(ave) ' is a function of α, β, and σ. DE P =DE P(ave) We can obtain α, β, and σ such that '.

[0050] More accurate estimated average density of produced oil and therefore estimated hydrogen consumption H C To obtain DE P(ave) and DE P(ave) It is preferable to compare the actual measured value of the average density of the produced oil over a certain period with the DE P(ave) (n), and the estimated average density of the produced oil is DE P(ave) '(n), where n represents the number of measured periods and is an integer equal to or greater than 2. For all n, DE P(ave) (n) / DE P(ave) It is preferable to obtain α, β, and σ such that '(n) is 0.9 to 1.1. The catalyst coefficients α, β, and σ may be obtained while carrying out the hydrotreating reaction in an actual reactor, or may be obtained in advance on a bench scale.

[0051] (f H Setting method 1) f H is calculated by using the estimated average density of the produced oil for the certain period calculated by the above formula 5, and the estimated hydrogen consumption H C is a tuning factor determined for each reactor when calculating

[0052] Tuning factor f H The method for obtaining this is not particularly limited, but it can be obtained by comparing with the actual measured value of hydrogen consumption over a certain period. An example will be described below. Using the above method, α, β, and σ are obtained, and the DEF(ave) and T information is obtained, and DE is calculated using Equation 5. P(ave) ' is calculated. Also, b1, b2, and b3 are obtained by the above method, and S F(ave) , S P(ave) , N.A. P(ave) , N.A. F(ave) , L, and the estimated hydrogen consumption H C In this case, H C is f H The actual measured value of hydrogen consumption for the given period, H RC =H C f such that H That is, in this embodiment, f H can be determined directly.

[0053] To obtain a more accurate estimated hydrogen consumption, the actual hydrogen consumption values ​​H RC and the estimated hydrogen consumption H C It is preferable to compare the actual measured value of hydrogen consumption for a certain period with H RC (n), and the estimated hydrogen consumption is H C (n), where n represents the number of measured periods and is an integer equal to or greater than 2. For all n, H RC (n) / H C f such that (n) is 0.9 to 1.1 H It is preferable to obtain the above. n is preferably 10 or more, and more preferably 20 or more. The certain period is not particularly limited, but may be, for example, 10 to 300 days. The tuning factor f H It is necessary to obtain this information on the actual device that will be used.

[0054] (f H Setting method 2) (f H Setting method 1) for tuning factors other than f H The following method can be used to obtain (f H In the setting method 1), b1, b2, and b3 were acquired in advance, but according to this method, f H, b1, b2, and b3 can be obtained simultaneously. Using the above method, α, β, and σ are obtained, and the DE F(ave) and T information is obtained, and DE is calculated using Equation 5. P(ave) ' is calculated. Also, S F(ave) , S P(ave) , N.A. P(ave) , N.A. F(ave) , L, and the estimated hydrogen consumption H C In this case, H C is b1, b2, B3(b3×f H ) is a function of the actual hydrogen consumption amount for the given period. RC =H C In other words, in this embodiment, it is possible to obtain b1, b2, and B3 such that H can be determined indirectly.

[0055] To obtain a more accurate estimated hydrogen consumption, the actual hydrogen consumption values ​​H RC and the estimated hydrogen consumption H C It is preferable to compare the actual measured value of hydrogen consumption for a certain period with H RC (n), and the estimated hydrogen consumption is H C (n), where n represents the number of measured periods and is an integer equal to or greater than 2. For all n, H RC (n) / H C It is preferable to obtain b1, b2, and B3 such that (n) is 0.9 to 1.1. n is preferably 10 or more, more preferably 20 or more. The certain period is not particularly limited, but may be, for example, 10 to 300 days. In this case, the tuning factors b1, b2, and B3 must be obtained from the actual device that will be used.

[0056] The estimated hydrogen consumption H obtained by the above formulas 1, 3, and 4 C and the measured hydrogen consumption value H RC In terms of the relationship with RC / H C is preferably 0.9 to 1.1. RC / HC If it is outside the above range, it is necessary to reset the various tuning parameters.

[0057] The above explanation is F(ave) , S P(ave) , N.A. P(ave) , N.A. F(ave) , A.R. F(ave) , A.R. P(ave) The explanation has been given on the assumption that the values ​​are measured values. In this case, the certain period is a period including a past period or a present period from the time when the information processing method of this embodiment is implemented. In the information processing method A described below, S F(ave) , S P(ave) is the assumed operating value. F(ave) and S P(ave) Based on NA P(ave) , N.A. F(ave) Calculate AR F(ave) (DE F(ave) ) is a characteristic derived from the feedstock, so it can be set to an assumed operating value by selecting the feedstock. P(ave) (DE P(ave) , D.E. P(ave) When calculating S′) from the above formulas 4 and 5, only the reaction temperature is required. P(ave) If it is possible to estimate a reaction temperature that can achieve the above, the information on the feedstock oil and the information on the product oil in the above formula 1 can be estimated rather than obtained by measurement. In this case, the certain period can be a future period from the time when the information processing method of this embodiment is implemented. That is, S can be calculated by the following information processing method A. F(ave) , S P(ave) , N.A. P(ave) , N.A. F(ave) , D.E. P(ave) ', DE F(ave) By obtaining this, it is possible to estimate the amount of hydrogen consumption for a certain period in the future.

[0058] <Information Processing Method A> The information processing method A of this embodiment includes the following steps for acquiring information about the feedstock, the product oil, and the operating conditions after a predetermined time has elapsed since the start of the hydrotreating reaction of a feedstock containing a diesel fraction (S1A in FIG. 2); a degradation calculation step (S2A in FIG. 2) for calculating the degradation level of the desulfurization reaction and the degradation level of the cracking reaction of the catalyst using a degradation function based on the acquired information about the feedstock, the product oil, and the operating conditions; a reaction temperature calculation step (S3A in FIG. 2) for calculating the reaction temperature required to satisfy the information about the feedstock, the product oil, and the operating conditions based on the degradation level of the desulfurization reaction of the catalyst; and a naphtha yield calculation step (S4A in FIG. 2) for calculating the naphtha yield based on the reaction temperature and the degradation level of the cracking reaction of the catalyst. Each step will be described below. Note that each step shown below is executed, for example, by the naphtha yield calculation device 2 of this embodiment. For example, S1A is executed by the acquisition unit 21, and S2A, S3A, and S4A are executed by the calculation unit 23 in the computer main body 22. Note that the information acquisition step is substantially the same as the information acquisition step described above, and therefore description thereof will be omitted.

[0059] <Deterioration level calculation step> The deterioration degree calculation step in this embodiment is a step of calculating the deterioration degree of the desulfurization reaction and the deterioration degree of the cracking reaction of the catalyst using a deterioration function based on the acquired information about the feedstock oil, information about the product oil, and information about the operating conditions. The step of calculating the degradation degree of the desulfurization reaction will be described below. The step of calculating the degradation degree of the decomposition reaction will be described later.

[0060] <Deterioration of desulfurization reaction> The deterioration degree of the desulfurization reaction is expressed by the following formula 6. Φ=k t / k0 expression 6 In the above formula 6, k0 is the reaction rate constant of the desulfurization reaction of the catalyst after 0 days of reaction (i.e., at the start of the reaction), and k t is the reaction rate constant of the desulfurization reaction of the catalyst after t days of reaction.t is the temperature T SOR is the reaction rate constant of the desulfurization reaction at

[0061] In this embodiment, the degree of deterioration of the desulfurization reaction of the catalyst can be calculated using the desulfurization reaction deterioration function based on the acquired information on the feedstock oil, information on the product oil, and information on the operating conditions.

[0062] <Degradation function 1 of desulfurization reaction> The desulfurization reaction deterioration function is a function for calculating the deterioration level of the desulfurization reaction of the catalyst. In this embodiment, the desulfurization reaction deterioration function is preferably a coke deterioration function relating to deterioration of the desulfurization reaction of the catalyst due to coke deposition. The coke deterioration function is not particularly limited as long as it is a function capable of calculating the deterioration level of the catalyst relating to coke deterioration. For example, the desulfurization reaction deterioration function 1 expressed by the following formula 7 can be mentioned as an example.

[0063] Φ=exp(-Dt) Equation 7 In the above formula 7, D is the deterioration coefficient of the active species of the desulfurization reaction of the catalyst, and t is the number of days elapsed since the reaction began.

[0064] D can be calculated using the following formula 8. Formula 8 below is an equation that can calculate the deterioration coefficient of the active species in the desulfurization reaction of the catalyst using specific parameters, and was first discovered by the inventors of the present application based on the operating results of an actual machine, etc.

[0065]

number

[0066] In this specification, the term "required temperature" refers to the reaction temperature required to achieve a predetermined reaction condition. That is, the required temperature on day 0 is the temperature at which the reaction starts. F , S P , LHSV, G、 and the reaction temperature required to achieve the reaction conditions P.

[0067] In this specification, the term "reference hydrogen partial pressure" refers to the standard pressure under actual reaction conditions. It is calculated as the average value of the reaction pressures used to determine the hydrogen partial pressure coefficient a, which will be described later.

[0068] In this specification, the "reference reaction temperature" refers to the T obtained under the standard operating conditions that may be actually used. SOR means the average value of

[0069] In this specification, the "reference hydrogen / feed oil ratio" refers to a standard hydrogen / feed oil ratio under actual reaction conditions. It is calculated as the average value of the hydrogen / feed oil ratios used to determine the hydrogen / feed oil ratio coefficient b, which will be described later.

[0070] In the formula 8, T SOR represents the initial activity of the catalyst for desulfurization, and α represents the deterioration rate of the catalyst for desulfurization. SOR The larger the value of α, the greater the deterioration of the catalyst's desulfurization reaction, and this deterioration behavior is reflected in the value of D.

[0071] In the above formula 8, (1 / S P n-1 -1 / S F n-1 ) The term expressed by LHSV is the desulfurization reaction rate constant, S P , S F When the LHSV is set as a set value and the operation is performed under certain conditions, it becomes a constant. B / P) a The term expressed by (G) is a term that indicates the hydrogen partial pressure dependency, and is a constant when P is set as a set value and operation is performed under constant conditions. B / G) b The term expressed by is a term that indicates the hydrogen / feed oil ratio dependency, and is a constant when G is set as a set value and operation is performed under constant conditions. In the above equation 8, exp[Ec / R(1 / T B -1 / T SOR )] is a term that indicates temperature dependency and is a constant.

[0072] In the formula 8, S F , S P , LHSV, P, and G are values ​​substituted based on the information on the feed oil, information on the product oil, and information on the operating conditions acquired in the information acquisition step described above. Note that LHSV can be calculated by dividing the feed oil supply rate (volume / h) by the catalyst loading rate (volume). G is the hydrogen supply rate (Nm 3 / hour) by the feed rate of the raw oil (kL / hour).

[0073] As mentioned above, S F , LHSV, P, and G are controllable parameters. P is the sulfur concentration of the target product oil. F , S P The depletion coefficient of the active species of the desulfurization reaction of the catalyst can be calculated under the reaction conditions of LHSV, P, and G. The method for determining n, which is the reaction order of the hydrotreating reaction of feedstock containing a diesel fraction, will be described later.

[0074] (How to determine basic degradation parameters) In the above formula 8, α, P B , a, G B ,b,Ec,T B , T SOR is a constant. Hereinafter, these parameters will be collectively referred to as "basic deterioration parameter 1." The basic deterioration parameter 1 is a parameter determined depending on the catalyst used, and may be determined while performing a reaction in an actual reactor, or may be determined in advance on a bench scale based on the operating conditions of the actual reactor. In this embodiment, it is preferable to determine the parameter in advance on a bench scale based on the operating conditions of the actual reactor. The basic degradation parameter P B , a, G B ,b,Ec,T B Here is an example of how to calculate P. The method of calculating P is based on the deterioration behavior of the catalyst desulfurization reaction (changes in the reaction rate constant of the desulfurization reaction) analyzed from data obtained from the reaction in the actual plant described above or from bench-scale reactions based on the operating conditions of the actual plant. B , a, G B ,b,Ec,T B (How to find α, T SOR Two examples of how to determine α and T are shown below, but the present invention is not limited to these. The first example is a method of determining α and T from the deterioration behavior of the desulfurization reaction of the catalyst (changes in the reaction rate constant of the desulfurization reaction) analyzed from data obtained from the reaction in the above-mentioned actual equipment or from a bench-scale reaction based on the operating conditions of the actual equipment. SOR The second example is a method to determine α and T from the reaction temperature profile analyzed from the data obtained from the reaction in the actual equipment or the bench-scale reaction based on the actual equipment operating conditions. SOR This is how to find it 2).

[0075] (P B , a, G B ,b,Ec,T B (How to find) The method for determining the basic deterioration parameters in this embodiment is based on the deterioration behavior of the desulfurization reaction of the catalyst analyzed from data obtained from the above-mentioned reaction in an actual plant or a bench-scale reaction under actual plant operating conditions. The deterioration behavior (degree of deterioration) of the desulfurization reaction of this catalyst can be expressed by the following equation 9, based on the same concept as equation 6. Φ'=k t ' / k0' expression 9 In the above formula 9, k0' is the reaction rate constant of the desulfurization reaction of the catalyst after 0 days of reaction (i.e., at the start of the reaction), and k t ' is the reaction rate constant of the desulfurization reaction of the catalyst after t days of reaction. t ' is the temperature T SOR ' is the reaction rate constant of the desulfurization reaction at

[0076] The above-mentioned formula 9 is a deterioration function based on the reaction rate constant of the desulfurization reaction, similar to the above-mentioned formula 6. The reaction rate constant is expressed by the Arrhenius equation shown in the following formula 10.

[0077]

number

[0078] Temperature T at the start of reaction SOR The reaction rate constant k0 of the desulfurization reaction in ' is k t In order to obtain an activity equivalent to the reaction rate constant k0' of the desulfurization reaction after t days of reaction, the reaction temperature must be set to T t ', the following formula 11 is derived from formulas 9 and 10. Note that, since the reaction in this embodiment is a hydrotreating reaction of a feedstock oil containing a light oil fraction, the activation energy E is set to the desulfurization activation energy Ea (kJ / mol).

[0079]

number

[0080] (Ec and T B (How to find) The LHSV, hydrogen partial pressure, hydrogen / feed oil ratio, and sulfur concentration in the feed oil are constant, and the sulfur concentration in the produced oil is set to a constant value S Pn The reaction is carried out for a certain period of time so that the sulfur concentration in the produced oil becomes S Pn To achieve this, the reaction temperature is increased while the reaction is carried out. If the reaction time is plotted on the horizontal axis and the measured reaction temperature on the vertical axis, and a regression line is drawn, y = a n x+b n (0 n ) is obtained. a n and b n is a value that reflects the catalyst deterioration behavior. n is T in the above formula 11 SOR In the above formula 11, T SOR ' to b n Substituting, T t By substituting the measured reaction temperature into ', the degradation degree Φ' of the desulfurization reaction after t days of reaction can be obtained. The activation energy Ea of desulfurization can be determined by the method described below. By plotting the logarithm of Φ' on the vertical axis and the reaction time on the horizontal axis, and drawing a regression line, y=-a n ’ x(|-a n ’ |=a n ’ ) is obtained. a n ’ represents the deterioration rate of the desulfurization reaction of the catalyst.

[0081] n types of sulfur concentration S Pn The same reaction is carried out for n a n , b n Then, using the same method as above, find n a n ’ ​where n is an integer of 3 or more. The larger the value of n, the more accurate Ec can be obtained. On the other hand, if the value of n is too large, it takes a long time to obtain Ec, which is not efficient. In this embodiment, n is preferably 3 to 20, and more preferably 3 to 10. The n a's obtained in this way n ’ and b n are substituted into the following formula 12. The following formula 12 is an equation that can calculate the activation energy of coke and the reference reaction temperature, and was first discovered by the inventors of the present application based on the operating results of an actual machine, etc.

[0082] ln(a n ’ )=ln(A)-(Ec / Rb n ) Equation 12 In Equation 12, A is the frequency factor, Ec is the activation energy of coke deterioration (kJ / mol), and R is the gas constant: 0.00831 (kJ / (mol·K)).

[0083] n a n ’ and b n For the combination of ln(a n ’ ) on the vertical axis, and 1 / b n On the horizontal axis, a regression line is drawn and its slope is calculated. Since this slope is Ec / R, the activation energy of coke deterioration, Ec, can be calculated by subtracting R from the slope.

[0084] Also, n b n By averaging T B can be obtained.

[0085] Ec and T B In determining the above, it is preferable that the LHSV, hydrogen partial pressure, hydrogen / feed oil ratio, and sulfur concentration in the feed oil are conditions that correspond to the operating conditions of the actual plant. Such LHSV is, for example, 0.3 to 2.0 h -1The hydrogen partial pressure is, for example, 3 to 7 MPa, and the hydrogen / feedstock ratio is, for example, 100 to 700 [Nm 3 / kL], and the sulfur concentration in the feed oil is, for example, 0.5 to 2.0 mass %. n types of sulfur concentration S Pn Similarly, it is preferable to set the conditions for S to match the actual operating conditions. Pn The content is, for example, 0.001 mass % or less. The reaction period is, for example, 30 to 1600 days.

[0086] (P B and how to find a) Under the conditions of constant LHSV, hydrogen / feed oil ratio, sulfur concentration in feed oil, and sulfur concentration in produced oil, the hydrogen partial pressure P m The reaction is carried out for a certain period of time under the conditions. Because the catalyst deteriorates during the reaction, the reaction temperature is increased to maintain a constant sulfur concentration in the resulting oil. If the reaction time is plotted on the horizontal axis and the measured reaction temperature on the vertical axis and a regression line is drawn, the equation becomes y=a m x+b m (0 m ) is obtained. On this line, b m is T in the above formula 11 SOR In the above formula 11, T SOR ' to b m Substituting, T t By substituting the actual reaction temperature into ', the degradation degree Φ' of the desulfurization reaction after any reaction time t days has elapsed can be obtained. By plotting the reaction time on the horizontal axis and the logarithm of Φ' on the vertical axis and drawing a regression line, y = -a m ’ x(|-a m ’ |=a m ’ ) is obtained. a m ’ represents the deterioration rate of the desulfurization reaction of the catalyst.

[0087] m types of hydrogen partial pressure P m The same reaction is carried out for m a m , b m ​Then, using the same method as above, m a m ’ where m is an integer of 3 or more. The larger the value of m, the more accurate a can be obtained. On the other hand, if the value of m is too large, it takes a long time to obtain a, which is not efficient. In this embodiment, m is preferably 3 to 20, and more preferably 3 to 10. The m a obtained in this way m ' and P m are substituted into the following equation 13. The following equation 13 is an equation that can calculate the hydrogen partial pressure coefficient and the reference hydrogen partial pressure, and was first discovered by the inventors of the present application based on the operating results of an actual machine, etc.

[0088] ln(a m ’ )=-aln(P m )+B1 Equation 13 In the formula 13, B1 can be 0.

[0089] m a m ' and P m For the combination of ln(a m ’ ) on the vertical axis, and ln(P m ) on the horizontal axis, draw a regression line, and determine its slope. This slope is the hydrogen partial pressure coefficient a.

[0090] In addition, the partial pressure P m By averaging P B can be obtained.

[0091] a and P B In determining the above, it is preferable that the LHSV, hydrogen / feed oil ratio, sulfur concentration in the feed oil, and sulfur concentration in the product oil are conditions that correspond to the operating conditions of the actual plant. Such LHSV is, for example, 0.3 to 2.0 h -1 The hydrogen / feedstock ratio is, for example, 100 to 700 [Nm 3 / kL], the sulfur concentration in the feed oil is, for example, 0.5 to 2.0 mass %, and the sulfur concentration in the product oil is, for example, 0.001 mass % or less. m hydrogen partial pressures P m Similarly, it is preferable to set the conditions for P to match the actual operating conditions. m The reaction pressure is, for example, 3 to 7 MPa. The reaction period is, for example, 30 to 1600 days.

[0092] (G B , how to find b) Under the conditions of constant LHSV, hydrogen partial pressure, sulfur concentration in feed oil, and sulfur concentration in the produced oil, the hydrogen / feed oil ratio G h The reaction is carried out for a certain period of time under the conditions. Because the catalyst deteriorates during the reaction, the reaction temperature is increased to maintain a constant sulfur concentration in the resulting oil. If the reaction time is plotted on the horizontal axis and the measured reaction temperature on the vertical axis, a regression line is drawn, which gives y=a h x+b h (0 h ) is obtained. On this line, b h is T in the above formula 11 SOR In the above formula 11, T SOR ' to b h Substituting, T t ’ By substituting the measured reaction temperature into , the degradation degree Φ' of the desulfurization reaction after any reaction time t days has elapsed can be obtained. By plotting the reaction time on the horizontal axis and the logarithm of Φ' on the vertical axis and drawing a regression line, y = -a h ’ x(|-a h ’ |=a h ’ ) is obtained. a h ’ represents the deterioration rate of the desulfurization reaction of the catalyst.

[0093] h types of hydrogen / feed oil ratio G h The same reaction is carried out for h a h , b h Then, using the same method as above, find h a h ’ ​h is an integer of 3 or more. The larger the value of h, the more accurate b can be obtained. On the other hand, if the value of h is too large, it takes a long time to obtain b, which is not efficient. In this embodiment, h is preferably 3 to 20, and more preferably 3 to 10. The h a obtained in this way h ' and G h are substituted into the following equation 14. The following equation 14 is an equation that can calculate the hydrogen / feed oil ratio coefficient and the reference hydrogen / feed oil ratio, and was first discovered by the inventors of the present application based on the operating results of an actual plant, etc.

[0094] ln(a h ')=-bln(G h )+B2 Equation 14 In the formula 14, B2 can be 0.

[0095] h a h ' and G h For the combination of ln(a h ') on the vertical axis, and ln(G h ) on the horizontal axis, draw a regression line, and determine its slope. This slope is the hydrogen / feed oil ratio coefficient b.

[0096] In addition, the above h types of hydrogen / feed oil ratio G h By averaging, G B can be obtained.

[0097] b and G B In determining the above, it is preferable that the LHSV, hydrogen partial pressure, sulfur concentration in the feed oil, and sulfur concentration in the product oil are conditions that correspond to the operating conditions of the actual plant. Such LHSV is, for example, 0.3 to 2.0 h -1 The hydrogen partial pressure is, for example, 3 to 7 MPa, the sulfur concentration in the feedstock oil is, for example, 0.5 to 2.0 mass %, and the sulfur concentration in the product oil is, for example, 0.001 mass % or less. h types of hydrogen / feed oil ratio G h Similarly, it is preferable to set the conditions for G according to the actual operating conditions. hFor example, 100 to 700 [Nm 3 / kL]. The reaction period is, for example, 30 to 1600 days.

[0098] (α and T SOR How to find 1) In an actual plant or on a bench scale, the reaction is carried out for a certain period of time so that the LHSV, hydrogen partial pressure, hydrogen / feed oil ratio, sulfur concentration in the feed oil, and sulfur concentration in the product oil are the assumed operating conditions of the actual plant. Because the catalyst deteriorates during the reaction, the reaction temperature is increased during operation. The assumed operating conditions of the actual plant are (Ec and T B (How to find P B and how to find a), (G B The operating conditions explained in (2) above are an example. If the reaction time is plotted on the horizontal axis and the measured reaction temperature on the vertical axis, and a regression line is drawn, y = a α x+b α A straight line expressed as a is obtained. α is a value correlated to α in the above formula 8, and b α is T in the above formula 8 SOR In the above formula 11, T SOR ' to b α Substituting, T t By substituting the actual reaction temperature into ', the degradation degree Φ' of the desulfurization reaction after any reaction time t days has elapsed can be obtained. By plotting the reaction time on the horizontal axis and the logarithm of Φ' on the vertical axis and drawing a regression line, y = -a α ’ x(|-a α ’ |=a α ’ ) is obtained. a α ’ represents the deterioration rate of the desulfurization reaction of the catalyst.

[0099] The operating condition is S P , S F , LHSV, P, G and P obtained by the above method B , a, G B ,b,Ec,T B、 T SOR (i.e., b α) into the above formula 8 to find D. Substituting the found D into the above formula 7 gives Φ. In this case, Φ is a function of α. If the reaction time is plotted on the horizontal axis and the logarithm of Φ on the vertical axis, and a regression line is drawn by changing α so that 0<α, then y=-α α ” x(|-a α ” |=a α ” ) are obtained for each value of α. α ” and the above-mentioned a α ’ can be set as α in the above-mentioned formula 8 when the values ​​are equal.

[0100] (α and T SOR How to find 2) (α and T SOR Carry out the same reaction as in 1) above, and find y=a α x+b α Obtain a line represented by b α T in the above formula 8 SOR The operating condition is S P , S F , LHSV, P, and P obtained by the above method B , a, G B ,b,Ec,T B、 T SOR (i.e., b α ) into the above formula 8 to find D. Substituting the found D into the above formula 7 gives Φ. In this case, Φ is a function of α. Substituting the found Φ into Φ' in the above formula 11, T SOR (i.e., b α ) in the above formula 11 SOR ’ Substituting into, T t ', T t ' is a function of α. The measured reaction temperature T obs T for t ' ratio (T t ' / T obs ) becomes 1 can be used as the α in the above formula 8. Similarly, N reaction temperatures T obs T for t ' ratio (Tt ' / T obs ) and the value of α when their average is closest to 1 is preferably used as α in the above formula 8. N is an integer of 10 or more, preferably 10 to 500, and more preferably 50 to 200.

[0101] <Degradation function of desulfurization reaction 2> In this embodiment, the coke deterioration function relating to the deterioration of the desulfurization reaction of the catalyst due to coke deposition is preferably deterioration function 2 expressed by the following equation 15, which is composed of an easily deactivated active species deterioration function relating to the deterioration of easily deactivated active species in the desulfurization reaction of the catalyst and a less easily deactivated active species deterioration function relating to the deterioration of less easily deactivated active species in the desulfurization reaction of the catalyst.

[0102] Φ=k1×exp(-D1t)+k2×exp(-D2t) Equation 15 In Equation 15, k1 is the activity site coefficient of the easily deactivated active species in the desulfurization reaction of the catalyst, k2 is the activity site coefficient of the resistant to deactivation active species in the desulfurization reaction of the catalyst, and the activity site coefficients represent the relative reaction rate constants of the desulfurization reaction of both active species. D1 is the deterioration coefficient of the easily deactivated active species in the desulfurization reaction of the catalyst, D2 is the deterioration coefficient of the resistant to deactivation active species in the desulfurization reaction of the catalyst, t is the number of days elapsed since the reaction began, and k1 + k2 = 1.

[0103] As described above, in the hydrotreating reaction of feedstock containing a diesel fraction, catalyst deterioration occurs due to coke deposition, and therefore, in order to maintain the sulfur content of the product oil below a certain level, it is necessary to operate the reactor at an elevated reaction temperature. In the hydrotreating reaction of feedstock containing a diesel fraction, the reaction temperature rises rapidly at the beginning of the reaction. This rapid rise in reaction temperature indicates rapid deterioration of the catalyst at the beginning of the reaction. On the other hand, from the middle of the reaction onwards, the reaction temperature rises gradually. This slow rise in reaction temperature indicates slow deterioration of the catalyst at the middle of the reaction onwards.

[0104] In other words, the profile of reaction temperature versus reaction time suggests that in the hydrotreating reaction of feedstock containing diesel fractions, rapid catalyst deterioration occurs at the beginning of the reaction, followed by gradual catalyst deterioration from the middle of the reaction onwards.

[0105] Based on the above-mentioned profile of reaction temperature versus reaction time, the inventors of the present application further improved deactivation function 1 and discovered deactivation function 2 on the assumption that the catalyst contains active species that are easily deactivated for the desulfurization reaction, which are deactivated in the early stage of the reaction, and active species that are difficult to deactivate for the desulfurization reaction, which are deactivated from the middle stage of the reaction onwards. As a result, they found that deactivation function 2 makes it possible to calculate the degree of deactivation of the catalyst's desulfurization reaction more accurately than deactivation function 1. The easily deactivated active species for the desulfurization reaction are active species that mainly lose activity in the early stage of the reaction, and the difficult to deactivate active species for the desulfurization reaction are active species that lose activity from the middle stage of the reaction onwards.

[0106] In the above formula 15, k1 represents the active site coefficient of the active species that is easily deactivated in the desulfurization reaction of the catalyst, and k2 represents the active site coefficient of the active species that is difficult to deactivate in the desulfurization reaction of the catalyst. k1 and k2 are constants specific to the catalyst, and their calculation methods will be described later.

[0107] D1 can be calculated using the following formula 16, and D2 can be calculated using the following formula 17.

[0108]

number

[0109]

number

[0110] In the formula 16 and the formula 17, S F is the sulfur concentration (mass%) in the feed oil after any reaction time t days, and S P is the sulfur concentration (mass%) in the product oil after t days of reaction, n is the reaction order of the hydrotreating reaction of the feedstock oil containing the light oil fraction, and LHSV is the liquid hourly space velocity (h -1 ) and P B is the reference hydrogen partial pressure (MPa), P is the hydrogen partial pressure (MPa) after any reaction t days have passed, a is the hydrogen partial pressure coefficient, and G B is the standard hydrogen / feed oil ratio (Nm 3 / kL), G is the hydrogen / feed oil ratio (Nm 3 / kL), b is the hydrogen / feed oil ratio coefficient, Ec is the activation energy of coke degradation (kJ / mol), R is the gas constant: 0.00831 (kJ / (mol K)), and T B is the reference reaction temperature (K), and T SOR is the required temperature (K) on day 0. In the above formula 16, α1 is the catalytic constant of the easily deactivated active site in the desulfurization reaction (a constant representing the degradation rate of the desulfurization reaction of the catalyst), and in the above formula 17, α2 is the catalytic constant of the hardly deactivated active site in the desulfurization reaction (a constant representing the degradation rate of the desulfurization reaction of the catalyst).

[0111] In the formula 16 and the formula 17, S F , S P , LHSV, P, and G are values ​​substituted based on the information on the feed oil, the information on the product oil, and the information on the operating conditions acquired in the information acquisition step, as in the explanation of Equation 8 above. Note that LHSV can be calculated by dividing the feed oil supply rate (volume / h) by the catalyst loading rate (volume). G is the hydrogen supply rate (Nm 3 / hour) by the feed rate of the raw oil (kL / hour).

[0112] As mentioned above, S F , LHSV, P, and G are controllable parameters. P is the sulfur concentration of the target product oil. That is, according to the above formulas 16 and 17, the above S F , S P The deactivation coefficient of the easily deactivated active species in the desulfurization reaction of the catalyst and the deactivation coefficient of the less easily deactivated active species in the desulfurization reaction of the catalyst can be calculated under the reaction conditions of , LHSV, and P. The method for determining n, which is the reaction order of the hydrotreating reaction of feedstock oil containing a diesel fraction, will be described later.

[0113] (How to determine basic degradation parameters) In the formula 16 and the formula 17, α1, α2, P B , a, G B ,b,Ec,T B, T SOR is a constant, as in the above-mentioned formula 8, and these parameters are collectively referred to as "basic deterioration parameter 2." The basic deterioration parameter 2 is a parameter determined depending on the catalyst used, and may be determined while carrying out a reaction in an actual machine, or may be determined in advance on a bench scale based on the operating conditions of the actual machine. In this embodiment, it is preferable to determine it in advance on a bench scale based on the operating conditions of the actual machine. In the above-mentioned formulas 16 and 17, P B , a, G B ,b,Ec,T B can be calculated in the same manner as in Equation 8 above. On the other hand, α1, α2, T SOR can be calculated by, for example, the following two methods. In addition, the activity site number coefficient k1 of the active species that is easily deactivated in the desulfurization reaction of the catalyst and the activity site number coefficient k2 of the active species that is difficult to deactivate in the desulfurization reaction of the catalyst in the above formula 15 can also be calculated at the same time as follows.

[0114] (α1, α 2、 T SOR 1) How to calculate k1 and k2 In an actual plant or on a bench scale, the reaction is carried out for a certain period of time so that the LHSV, hydrogen partial pressure, hydrogen / feed oil ratio, sulfur concentration in the feed oil, and sulfur concentration in the product oil are the expected operating conditions of the actual plant. Because the catalyst deteriorates during the reaction, the reaction temperature is increased during operation. The reaction time is plotted on the horizontal axis and the reaction temperature on the vertical axis. When drawing a regression line for these plots, as mentioned above, the initial reaction time (x1 to x n ) is a straight line expressed as y=a1x+b1, which correlates with the rapid rise in reaction temperature, and the line expressed as y=a1x+b1 after the middle stage of the reaction (x n+1 ~x m ) Two straight lines are obtained, which are expressed as y = a2x + b2, which correlate with the gradual increase in reaction temperature. In the above equation, a1 > a2 > 0, and b1 <b2であり、x1<x n <x n+1 <x m x n , x m means the reaction time relative to the n(m)th plot from the start of the reaction.

[0115] The above-mentioned a1 is a value correlated with α1, b1 is a value correlated with k1+k2, and T SOR In addition, a2 is a value that correlates with α2, and b2 is a value that correlates with k2. Next, the intersection point (x ip , y ip ) is calculated. This intersection point means the inflection point of y=a1x+b1 and y=a2x+b2. That is, (x ip , y ip ), it is assumed that only active species that are easily deactivated in the desulfurization reaction of the catalyst exist, and (x ip , y ip ) is considered to have two active species: one that is easily deactivated in the desulfurization reaction of the catalyst and one that is difficult to deactivate in the desulfurization reaction of the catalyst.

[0116] In the formula 11, T SOR ' is assigned to b1, and T t By substituting the reaction temperature into ', the degradation degree Φ' of the desulfurization reaction after any reaction time t days has elapsed can be obtained. Plot the reaction time on the horizontal axis and the logarithm of Φ' on the vertical axis, and then calculate the values ​​of x1 to x ip If we draw a regression line up to y=-a1 ’ x (|-a1 ’ |=a1 ’ ) is obtained. Also, x ip ~x m If we draw a regression line to y=-a2 ’ x-b2 ’ (|-a2 ’ |=a2 ’ and |-b2 ’ |=b2 ’ ) is obtained. a1 ’ is a value correlated with α1, and a2 ’ is a value correlated with α2, and b2 ’ is a value correlated to k2.

[0117] k2 is the b2 obtained from the regression line above. ’ can be calculated by substituting into the following equation 18. Since k1 is k1+k2=1, it can be calculated from k1=1-k2. k2=exp(-b2 ’) Equation 18

[0118] The operating condition is S P , S F , LHSV, P, G and P obtained by the above method B , a, G B ,b,Ec,T B , T SOR Substituting (b1) into the above formula 16 and formula 17 gives D1 and D2. Substituting the obtained D1, D2, k1, and k2 into the above formula 15 gives Φ. In this case, Φ is a function of α1 and α2. Plot the reaction time on the horizontal axis and the logarithm of Φ on the vertical axis, and set α2 = 0 and change α1 so that 0 < α1 to obtain x1 to x ip If we draw a regression line from y to -a α1 ” x(|-a α1 " |=a α1 ” ) are obtained for each value of α1. α1 ” and the above-mentioned a1 ’ The α1 when these values ​​are equal can be used as the α1 in the above equation (16). Next, substitute the obtained α1 into Φ, which is a function of α1 and α2 obtained by the above method, and change α2 so that 0<α2 to obtain x ip ~x m If we draw a regression line from y to -a α2 ” xb α2 " (|-a α2 ” |=a α2 " ) are obtained for each value of α2. α2 and the above-mentioned a2 ’ The α2 when these values ​​are equal can be used as the α2 in the above equation 17.

[0119] (α1, α 2、 T SOR 2) How to calculate k1 and k2 (α1, α 2、 T SOR, k1, and k2. SOR (b1) is obtained. The operating condition is S P , S F , LHSV, P, and P obtained by the above method B ,a,Ec,T B , T SOR (b1) is substituted into the above formula 16 and formula 17 to obtain D1 and D2. The obtained D1 and D2 are substituted into the above formula 15 to obtain Φ. In this case, Φ is a function of α1, α2, k1, and k2. The obtained Φ is substituted into Φ' in the above formula 11, and T SOR (i.e., b1) is T in the above formula 11 SOR ’ Substituting into, T t ', T t ' is a function of α1, α2, k1, and k2. If α2 is set to 0 and k2 = 1-k1, then T t ' is a function of α1 and k1. x1~x ip The measured reaction temperature T obs T for t ' ratio (T t ' / T obs ) is 1, and this α1 can be used as α1 in the above formula 16. Note that k1 at this time is a tentative value. Similarly, M reaction temperatures T obs T for t ' ratio (T t ' / T obs ) and the α1 at which their average is closest to 1 is preferably taken as the α1 in the above formula 16. M is an integer of 10 or more, preferably 10 to 500, and more preferably 50 to 200. Using the obtained α1, let k1 = 1-k2, and T t ' is a function of α2 and k2. x ip ~x m The measured reaction temperature T obs T for t ' ratio (Tt' / T obs) is 1, the combination of α2 and k2 can be determined, and these α2 and k2 can be used as α2 and k2 in the above formula 17. By substituting the obtained k2 into k1 = 1 - k2, k1 can be determined, and this k1 can be used as k1 in the above formula 16. Similarly, obs T for t ' ratio (T t ' / T obs ) and use α2 and k2 when their average is closest to 1 as α2 and k2 in the formula 17. Also, use k1 calculated from the obtained k2 as k1 in the formula 16. L is an integer of 10 or more, preferably 10 to 500, and more preferably 50 to 200.

[0120] In this way, α1, α 2、 T SOR , k1, and k2, it is necessary to obtain y=a1x+b1 and y=a2x+b2. For example, y=a1x+b1 and y=a2x+b2 can be obtained as follows.

[0121] Using the method described above, plot the reaction time on the horizontal axis and the reaction temperature on the vertical axis. A regression line is drawn from the start of the reaction to the end of the reaction, resulting in a line expressed as y = a'x + b'. This line does not take into account the inflection point. Remove plots from the end of the reaction in order, and adjust the y = a'x + b' so that the correlation coefficient approaches 1, to obtain y = a1'x + b1'. Similarly, remove plots from the start of the reaction in order, and adjust the y = a'x + b' so that the correlation coefficient approaches 1, to obtain y = a2'x + b2'. The lines where the average correlation coefficients of y = a1'x + b1' and y = a2'x + b2' are closest to 1 are y = a1x + b1 and y = a2x + b2. All plots should belong to either y = a1x + b1 or y = a2x + b2.

[0122] The reaction time required to obtain y = a1x + b1 and y = a2x + b2 is usually 100 days or more. In general, it is sufficient to carry out the reaction until the correlation function of y = a'x + b' becomes 0.5 or greater.

[0123] <Reaction temperature calculation step> The reaction temperature calculation step of this embodiment is a step of calculating a reaction temperature necessary to satisfy the information on the feedstock oil, the information on the product oil, and the operating conditions based on the degree of deterioration of the desulfurization reaction of the catalyst. The reaction temperature is preferably calculated using a desulfurization rate equation based on the Arrhenius equation.

[0124] <Degradation rate equation for desulfurization reaction> The deterioration rate equation for the desulfurization reaction is based on the Arrhenius equation expressed by the above-mentioned equation 10. Similar to the calculation method for the above-mentioned equation 11, the following equation 19 is derived from the above-mentioned equations 6 and 10.

[0125]

number

[0126]

number

[0127] In the above formula 20, T obtained by the above method SOR , Φ, T after t days of any reaction t (K) can be obtained. The activation energy of the desulfurization reaction in the above formula 20 can be calculated as follows.

[0128] (How to calculate the activation energy of the desulfurization reaction) The activation energy of the desulfurization reaction can be determined by a method known in the art based on the Arrhenius equation represented by the above-mentioned formula 10. An example will be described below.

[0129] First, determine the reaction order of the desulfurization reaction of feedstock containing diesel fraction. The reaction temperature, hydrogen partial pressure, hydrogen / feedstock ratio, and sulfur concentration in the feedstock are kept constant, and the reaction is carried out under the conditions of LHSV(x), and the sulfur concentration in the resulting oil is measured. S in the desulfurization reaction rate equation, expressed as Equation 21 below, is F The sulfur concentration in the feed oil is expressed as S P Substitute LHSV(x) for the sulfur concentration in the resulting oil obtained in . Plot the result on the left side of the equation on the vertical axis and 1 / LHSV on the horizontal axis. In this case, the vertical axis is a function of n.

[0130]

number

[0131] The same reaction is carried out for x types of LHSV(x), and x plots of the above are obtained. Based on the obtained plots, a regression line is drawn through the origin to obtain a line expressed as y = cx. y is (1 / n-1((1 / S P n-1 )-(1 / S F n-1 ))), where x is 1 / LHSV and c is k. Calculate the correlation function using Excel or similar software and find the n that makes the correlation coefficient closest to 1. The resulting n is the reaction order. Note that n should be calculated to the first decimal place.

[0132] The above x is an integer of 3 or more. The larger the number of x, the more accurate n can be obtained. On the other hand, if the number of x is too large, it takes a long time to obtain n, which is not efficient. In this embodiment, x is preferably 3 to 20, and more preferably 3 to 10.

[0133] In determining n, the reaction temperature, hydrogen partial pressure, hydrogen / feedstock ratio, and sulfur concentration in the feedstock are preferably set to conditions that correspond to the operating conditions of an actual plant. The reaction temperature is, for example, 300 to 400°C, the hydrogen partial pressure is, for example, 3 to 7 MPa, and the hydrogen / feedstock ratio is, for example, 100 to 700 [Nm 3 / kL], and the sulfur concentration in the feed oil is, for example, 0.5 to 2.0 mass %. Similarly, it is preferable that the x types of LHSV(x) are set to conditions that correspond to the actual operating conditions. For example, LHSV(x) is set to 0.3 to 2.0 h -1 is.

[0134] When the activation energy E in the Arrhenius equation expressed by the above formula 10 is set to the activation energy Ea of desulfurization and the natural logarithm of both sides is taken, the following formula 22 is obtained.

number

[0135] The hydrogen partial pressure, hydrogen / feed oil ratio, LHSV, and sulfur concentration in the feed oil are kept constant, and the reaction is carried out at a reaction temperature of T(y), and the sulfur concentration in the resulting oil is measured. F The sulfur concentration in the feed oil is expressed as S P The sulfur concentration in the product oil obtained in is substituted for LHSV, and the above obtained n is substituted to determine the reaction rate constant k. The obtained reaction rate constant is substituted into the above equation 22, and the result (lnk) on the left side obtained is plotted on the vertical axis and 1 / T (1 / T(y)) on the horizontal axis.

[0136] The same reaction is carried out at y different reaction temperatures T(y), and y plots like the one above are obtained. A regression line is drawn from the obtained plots, and its slope is determined. Since this slope is Ea / R, the activation energy of desulfurization, Ea, can be calculated by subtracting R from the slope.

[0137] The above y is an integer of 3 or more. The larger the number of y, the more accurate Ea can be obtained. On the other hand, if the number of y is too large, it takes time to obtain Ea, which is not efficient. In this embodiment, y is preferably 3 to 20, and more preferably 3 to 10.

[0138] In determining Ea, the hydrogen partial pressure, hydrogen / feed oil ratio, LHSV, and sulfur concentration in the feed oil are preferably set to conditions that correspond to the operating conditions of the actual plant. The hydrogen partial pressure is, for example, 3 to 7 MPa, and the hydrogen / feedstock ratio is 100 to 700 [Nm 3 / kL] and LHSV is 0.3 to 2.0 h -1 The sulfur concentration in the feed oil is 0.5 to 2.0 mass %. Similarly, it is preferable that the reaction temperature T(y) of the y types is set to a condition that conforms to the operating conditions of the actual equipment. Such T(y) is 300 to 400°C.

[0139] By substituting each parameter thus obtained into the above-mentioned formula 20, the reaction temperature T required to achieve the predetermined reaction conditions can be calculated. t can be obtained.

[0140] Actual reaction temperature T obs The reaction temperature T obtained by the information processing method of this embodiment t T is the ratio of t / T obs is preferably 0.97 to 1.03, and more preferably 0.985 to 1.015, in °C. t / T obs If is within the above range, it can be determined that the reaction temperature can be estimated with high accuracy.

[0141] <Naphtha yield calculation step> In the naphtha yield calculation step of this embodiment, t The naphtha yield is calculated based on the degree of deterioration of the catalyst cracking reaction. The naphtha yield is preferably calculated using a naphtha yield calculation function based on a first-order cracking reaction rate equation.

[0142] <Naphtha yield calculation function> The naphtha yield calculation function is expressed by the following equation 23.

[0143]

number

[0144] In the above-mentioned formula 23, LHSV is a value substituted based on the information on the operating conditions acquired in the above-mentioned information acquisition step. Note that LHSV can be calculated by dividing the feed oil supply rate (volume / h) by the catalyst loading amount (volume). Φ C and k C0(Tt) The method for calculating this will be described later.

[0145] As described above, NA in Equation 1 P(ave) is the average naphtha concentration in the produced oil for the given period, and NA F(ave) is the average naphtha concentration in the feed oil during the given period. Here, the naphtha concentration in the product oil after any reaction day t during the given period is expressed as NA P , the concentration of naphtha in the feed oil is NA F The diesel fraction does not contain naphtha (NA F =0), then (NA P -NA F ) is NA P Furthermore, if we consider that naphtha is produced by the cracking reaction of diesel fraction, then NA P is the amount of naphtha obtained, C t (% by mass). That is, according to this embodiment, (NA P -NA F )=C t This becomes:

[0146] The degradation degree of the decomposition reaction in the above formula 23 is expressed by the following formula 24. ΦC =k Ct(T0) / k C0(T0) formula 24 In the formula 24, k C0(T0) is the reaction rate constant of the decomposition reaction of the catalyst (fresh catalyst) at the beginning of the reaction (i.e., at the start of the reaction), and k Ct(T0) is the reaction rate constant of the catalyst decomposition reaction after t days of reaction. Ct(T0) , k C0(T0) is the temperature T SOR is the reaction rate constant for the decomposition reaction at

[0147] The above-mentioned formula 23 is derived based on the premise that the cracking reaction of diesel is a first-order reaction and that naphtha is produced by the cracking reaction. The method for deriving the above-mentioned formula 23 will be explained below.

[0148] The decomposition reaction rate equation is expressed as Equation 25 below. k Ct(Tt) =ln(C F / C P )×LHSV Equation 25 In the formula 25, k Ct(Tt) is the reaction temperature T calculated in the above reaction temperature calculation step after any reaction t days have passed. t The reaction rate constant (h -1 ) and C F is the diesel concentration (mass%) in the feedstock oil after any reaction time t days, and C P is the diesel concentration (mass%) in the produced oil after t days of reaction, and LHSV is the liquid hourly space velocity (h -1 )

[0149] C F / C P is dimensionless, so C F If is set to 1, the conversion rate C of the decomposition reaction after any reaction time t days has elapsed t (%) is C t =(1-C P ) × 100. Therefore, C P is C P= 1-Ct / 100. As mentioned above, based on the assumption that naphtha is produced by the cracking reaction, the conversion rate C t (%) is also the amount of naphtha obtained (mass%). Substituting these into Equation 25 above, we obtain Equation 26 below.

[0150]

number

[0151]

number

[0152] Φ C =k Ct(Tt) / k C0(Tt) formula 28 In the formula 28, k C0(Tt) is the reaction rate constant of the decomposition reaction of the catalyst (fresh catalyst) at the beginning of the reaction (i.e., at the start of the reaction), and k Ct(Tt) is the reaction rate constant of the catalyst decomposition reaction after t days of reaction. Ct(Tt) , k C0(Tt) is the reaction temperature T calculated in the reaction temperature calculation step above after t days of reaction. t is the reaction rate constant for the decomposition reaction at

[0153] From the above formula 28, k Ct(Tt) =Φ C ×k C0(Tt) By substituting this value into the above-mentioned equation 27, the above-mentioned equation 23 is derived.

[0154] Next, Φ C , k C0(Tt) We will explain how to find this.

[0155] (k C0(Tt) (How to find) k C0(Tt)is a parameter (constant) determined depending on the catalyst used, and may be determined while carrying out a reaction in an actual reactor, or may be determined in advance on a bench scale based on the operating conditions of the actual reactor. In this embodiment, it is preferable to determine it in advance on a bench scale based on the operating conditions of the actual reactor. k C0(Tt) can be calculated by the following formula 29. The following formula 29 is based on the Arrhenius equation expressed by the above formula 10.

[0156]

number

[0157] k C0(T0) is the reaction temperature T of the fresh catalyst SOR Since this is the reaction rate constant of the decomposition reaction in the above formula 26, it can be calculated by the following formula 30.

[0158]

number

[0159] That is, k C0(T0)is a bench scale reaction using fresh catalyst at the reaction temperature of T SOR The hydrotreating reaction is carried out at the LSHV, which is the operating condition of the actual plant, and the naphtha yield is measured, and the yield can be calculated from the above formula (30).

[0160] On the above bench scale, k C0(T0) When calculating the above, it is preferable that the hydrogen partial pressure, hydrogen / feed oil ratio, LHSV, and sulfur concentration in the feed oil are set to conditions that correspond to the operating conditions of the actual plant. The hydrogen partial pressure is, for example, 3 to 7 MPa, and the hydrogen / feedstock ratio is 100 to 700 [Nm 3 / kL] and LHSV is 0.3 to 2.0 h -1 The sulfur concentration in the feed oil is 0.5 to 2.0 mass %.

[0161] k C0(T0) can be calculated while the reaction is running in the actual equipment as follows: int Reaction temperature T int The amount of naphtha obtained and the LHSV can be calculated by substituting them into the above formula 30. int The time is preferably 20 days or less, and more preferably 10 days or less. int When T is equal to or less than the upper limit, a value very close to the reaction rate constant of the decomposition of the fresh catalyst can be obtained. int is a value calculated from the deterioration degree of the desulfurization reaction by the reaction temperature calculation step described above.

[0162] Activation energy of decomposition E D can be found as follows:

[0163] The activation energy E in the Arrhenius equation represented by Equation 10 is the decomposition activation energy E D Taking the natural logarithm of both sides gives us the following equation (31).

number

[0164] The activation energy of decomposition can be determined by carrying out the reaction in an actual plant, or based on the operating conditions of the actual plant. The reaction rate constant k can be calculated in advance on a bench scale based on the above equation. The hydrogen partial pressure, hydrogen / feedstock ratio, LHSV, and sulfur concentration in the feedstock are kept constant, and the reaction is carried out at a reaction temperature of T(y'), and the naphtha yield in the product oil is measured. The naphtha yield and LHSV obtained are substituted into equation 26 to calculate the reaction rate constant k. The obtained reaction rate constant is substituted into equation 31, and the result (lnk) on the left side of the equation is plotted on the vertical axis and 1 / T (1 / T(y')) on the horizontal axis.

[0165] The same reaction is carried out for y' kinds of reaction temperatures T(y'), and y' plots are obtained. A regression line is drawn from the obtained plots, and its slope is calculated. This slope is E D / R, so by subtracting R from the slope, the activation energy of decomposition, E D can be obtained.

[0166] The above y' is an integer equal to or greater than 3. The larger the number of y', the more accurate the E D On the other hand, if the number of y' is too large, E D In this embodiment, y' is preferably 3 to 20, and more preferably 3 to 10.

[0167] E D In determining the above, it is preferable that the hydrogen partial pressure, hydrogen / feed oil ratio, LHSV, and sulfur concentration in the feed oil are conditions that correspond to the operating conditions of the actual plant. The hydrogen partial pressure is, for example, 3 to 7 MPa, and the hydrogen / feedstock ratio is 100 to 700 [Nm 3 / kL] and LHSV is 0.3 to 2.0 h -1 The sulfur concentration in the feed oil is 0.5 to 2.0 mass %. Similarly, it is preferable that the reaction temperature T(y') of the y' types is set to a condition that conforms to the operating conditions of the actual equipment. Such T(y') is 300 to 400°C.

[0168] The k obtained in this wayC0(T0) , the activation energy of decomposition E D , T SOR , the reaction temperature T calculated in the reaction temperature calculation step described above t By substituting into the above equation 29, k C0(Tt) Ask for.

[0169] <Deterioration of decomposition reaction> When the desulfurization reaction activity of the catalyst decreases, the cracking reaction activity also decreases. Therefore, it is thought that there is a correlation between the degree of deterioration of the desulfurization reaction and the degree of deterioration of the cracking reaction. The inventors of the present application focused on this correlation and calculated the degree of deterioration of the cracking reaction Φ C It was found for the first time that the degradation degree Φ of the desulfurization reaction can be calculated based on the above-mentioned degradation degree Φ of the desulfurization reaction. C We will explain how to find each of these.

[0170] (Method 1 for determining the degree of degradation of decomposition reactions) Φ C The method for calculating Φ is based on the degradation function 1 of the desulfurization reaction. C This is a method to find Φ C can be calculated using the following equation 32.

[0171] Φ C =βΦ Equation 32 In the above formula 32, Φ C is the degradation degree of the decomposition reaction, Φ is the degradation degree of the desulfurization reaction (degradation function 1 of the desulfurization reaction), and β is the degradation coefficient of the decomposition reaction (constant).

[0172] Since Φ can be calculated using the method described above, once β is determined, Φ can be calculated from C In the above formula 32, Φ at the time of reaction elapsed time 0 can be calculated. C where βΦ=1.

[0173] In an actual plant or on a bench scale, the reaction is carried out for a certain period of time so that the LHSV, hydrogen partial pressure, hydrogen / feed oil ratio, sulfur concentration in the feed oil, and sulfur concentration in the product oil are the assumed operating conditions of the actual plant. Because the catalyst deteriorates during the reaction, the reaction temperature is increased during operation. The reaction temperature at this time is calculated by the reaction temperature T calculated in the reaction temperature calculation step described above. t The assumed operating conditions for the actual plant are the conditions used to calculate the activation energy of the cracking process mentioned above. The amount of naphtha obtained after t' days of reaction, C, is t’ Measure the resulting C t’ , k obtained by the above method C0(Tt) (k C0(Tt’) ), and LHSV are substituted into Equation 23, C Also, using the above method, Φ is calculated after t' days of any reaction. Similarly, Φ is calculated for multiple reactions after t' days. C and Φ are calculated. Φ C For the combination of and Φ, Φ is on the x-axis, and Φ C The y-axis is used to plot the values. A regression line is drawn between these plots (where x=0 and y=0). The slope of this line is β. The number of plots used to determine β is preferably 10 to 100, and more preferably 10 to 50. Furthermore, the value of t' used to determine β is preferably after 3 days of reaction.

[0174] (Method 2 for determining the degree of degradation of decomposition reactions) Φ C The method 2 for determining Φ is based on the degradation function 2 of the desulfurization reaction. C This is a method to find Φ C can be calculated using the following equation 33.

[0175] Φ C =β1Φ1+β2Φ2 Equation 33 In the above formula 33, Φ Cis the degree of deterioration of the decomposition reaction, Φ1 is k1 × exp(-D1t) in equation 15, Φ2 is k2 × exp(-D2t) in equation 15, β1 is the decomposition deterioration coefficient (constant) of the easily deactivated active species of the catalyst, and β2 is the decomposition deterioration coefficient (constant) of the hardly deactivated active species of the catalyst.

[0176] Since Φ1 and Φ2 can be obtained by the above method, once β1 and β2 are determined, Φ C In the above formula 33, Φ at the time of reaction elapsed time 0 can be calculated. C is β1Φ1+β2Φ2=1.

[0177] In an actual plant or on a bench scale, the reaction is carried out for a certain period of time so that the LHSV, hydrogen partial pressure, hydrogen / feed oil ratio, sulfur concentration in the feed oil, and sulfur concentration in the product oil are the assumed operating conditions of the actual plant. Because the catalyst deteriorates during the reaction, the reaction temperature is increased during operation. The reaction temperature at this time is calculated by the reaction temperature T calculated in the reaction temperature calculation step described above. t The amount of naphtha obtained after any reaction t' days has elapsed is C t’ Measure the resulting C t’ , k obtained by the above method C0(Tt) (k C0(Tt’) ), and LHSV are substituted into Equation 23, C Also, using the above method, Φ1 and Φ2 are calculated after t' days of reaction. C , Φ1, Φ2 are substituted into the above formula 33. Similarly, Φ Cn , Φ 1n , Φ 2n If Equation 33 holds for each combination, then Φ Cn =β1'Φ 1n +β2'Φ 2n In this equation, Φ Cn is the dependent variable, Φ 1n、 and Φ 2nThe β1' and β2' with the smallest error can be obtained by two-way linear regression with β as the independent variables. The obtained β1' can be used as β1 in the above formula 33, and the obtained β2' can be used as β2 in the above formula 33. In obtaining β1 and β2, Φ C The number of combinations of Φ1 and Φ2 is preferably 10 to 100, more preferably 10 to 50. In addition, the time t' for determining β1 and β2 is preferably 3 days or more after the reaction.

[0178] Using the β or β1 and β2 obtained by the above method, Φ is calculated from the above formula 32 or 33. C can be obtained.

[0179] The k obtained by the above method C0(Tt) , Φ calculated by the above-mentioned formula 32 or the above-mentioned formula 33 C By substituting the above formula 23, the yield of naphtha after t days of reaction can be calculated.

[0180] Actual naphtha yield C obs The naphtha yield C obtained by the information processing method of this embodiment t C is the ratio of t / C obs is preferably 0.80 to 1.20, more preferably 0.85 to 1.15, in terms of mass %. t / C obs When the amount of naphtha obtained is within the above range, it can be determined that the amount of naphtha obtained can be estimated with high accuracy.

[0181] From the above, S F , S P is the set point, and the reaction temperature T required to achieve this set point is t Also, the naphtha yield (C t During the certain period, S F , S P is set as a constant value, and that value is S F(ave) , S P(ave) In addition, during the certain period, Ct (NA P -NA F ) and calculate the average (NA P(ave) -NA F(ave) ) can be set. Furthermore, during the certain period, DE F is set as a constant value, and that value is DE F(ave) Furthermore, in the certain period, T t and the estimated density of the produced oil after any reaction time t days has elapsed is calculated using Equation 5. P ' and calculate the average P(ave) ' can be used. The method may further include an information output step (S5A in FIG. 2) for outputting the information calculated by the information processing method A of this embodiment. Also, the information may be output (transmitted) to the information acquisition step of the information processing method of the present invention. For example, S5A is executed by the output unit 24. Note that the S obtained by the information processing method of this embodiment F , S P , N.A. P , N.A. F , D.E. F , D.E. P ' is information after t days have passed from any reaction, and it is sufficient that this time after t days has passed is included in the certain period.

[0182] Actual hydrogen consumption H RC The hydrogen consumption H calculated by the information processing method of this embodiment C is the ratio of H C / H RC is Nm 3 In terms of conversion, the H is preferably 0.85 to 1.15, and more preferably 0.9 to 1.1. C / H RC If is within the above range, it can be determined that the hydrogen consumption amount can be estimated with high accuracy.

[0183] <Information output step> The method may further include an information output step (S3 in FIG. 1) of outputting information indicating the amount of hydrogen consumed in the hydrotreating reaction calculated in this manner. For example, S3 is executed by the output unit 14.

[0184] <Hydrotreatment reaction of feedstock containing diesel fraction> The hydrotreating reaction of feedstock containing diesel fractions will be outlined below. In this specification, the term "diesel fraction" refers to a boiling point range of 150 to 380°C, and includes, for example, catalytically cracked diesel oil, thermally cracked diesel oil, hydrotreated diesel oil, desulfurized diesel oil, and mixtures thereof, which are obtained by subjecting straight-run diesel oil and heavy oil obtained by atmospheric distillation of crude oil to catalytic cracking, thermal cracking, hydrotreating, and desulfurization, respectively, followed by fractional distillation. The content of the diesel fraction in the feedstock may be, for example, 50% by volume or more, or 80% by volume or more. Incidentally, fractions other than the light oil fraction contained in the feedstock include naphtha and the like.

[0185] In this specification, "naphtha" refers to a component having a boiling point range of 175°C or less and having 5 to 10 carbon atoms, which is obtained by cracking in a hydrotreating reaction. In this specification, the term "aromatic compound" refers to a cyclic unsaturated organic compound, and among these, a compound having 1 to 3 or more rings.

[0186] The hydrotreating reaction of a feedstock containing a gas oil fraction can be carried out by contacting the feedstock containing a gas oil fraction with a hydrotreating catalyst. The hydrotreating catalyst is not particularly limited, and any hydrotreating catalyst known in the art can be used. Various catalyst supports can be used, including, for example, silica, alumina, boria, magnesia, titania, silica-alumina, silica-magnesia, silica-zirconia, silica-thoria, silica-beryllia, silica-titania, silica-boria, alumina-zirconia, alumina-titania, alumina-boria, alumina-chromia, titania-zirconia, silica-alumina-thoria, silica-alumina-zirconia, silica-alumina-magnesia, silica-magnesia-zirconia, and the like, or mixtures of two or more of these. Among these inorganic oxides, preferred are alumina, silica-alumina, alumina-titania, alumina-boria, and alumina-zirconia, with alumina being particularly preferred, and gamma alumina being particularly preferred. These inorganic oxides may be used alone or in combination of two or more.

[0187] The metal contained in the support as an active component is at least one metal selected from Group 6 metals and Groups 8 to 10 metals of the periodic table, preferably molybdenum, tungsten, cobalt, and nickel. These metals are effective in the metallic state, metal oxide, or metal sulfide form. They may also be bonded to the catalyst support by ion exchange or other methods. The content of this metal component is typically within the range of approximately 10 to 25 mass% of the catalyst, calculated as oxide. If the metal content is less than 10 mass%, the absolute amount of metal acting as active sites is small, and hydrotreating activity (hereinafter simply referred to as hydrotreating activity), including desulfurization activity, is not achieved. Conversely, if the supported metal content is greater than 25 mass%, metal aggregation occurs, reducing the number of active sites and, as a result, hydrotreating activity is actually reduced. Furthermore, if necessary, phosphorus, boron, zinc, zirconia, etc. can be contained in addition to the active metals consisting of Group 6 and Group 8 metals of the periodic table. When applying the method of the present invention, there is no restriction on the form of the catalyst bed, and it can be applied to reactors with catalyst beds such as fixed beds, moving beds, and fluidized beds.

[0188] The conditions for the hydrotreating reaction of feedstock containing a light oil fraction are generally a reaction temperature of 300 to 400°C, preferably 330 to 380°C, a hydrogen partial pressure of 3 to 7 MPa, preferably 4 to 6 MPa, and a liquid hourly space velocity of 0.3 to 2 h -1 , preferably 0.5 to 1.5 hours -1 The hydrogen / feed oil ratio is 100 to 700 [Nm 3 / kL], preferably 200 to 500 [Nm 3 / kL].

[0189] <Hydrogen consumption calculation device> The hydrogen consumption calculation device of this embodiment includes an acquisition unit that acquires information about a feedstock containing a light oil fraction and information about a product oil over a certain period of time regarding a hydrotreatment reaction of the feedstock containing a light oil fraction, and a calculation unit that calculates the amount of hydrogen consumed in the hydrotreatment reaction over the certain period of time based on the information about the feedstock and the information about the product oil acquired by the acquisition unit. The hydrogen consumption calculation device of this embodiment may also have an output unit that outputs information about the calculated amount of hydrogen consumed in the hydrotreatment reaction over the certain period of time.

[0190] The naphtha yield calculation device of this embodiment includes an acquisition unit that acquires information about the feedstock, information about the product oil, and information about operating conditions after a predetermined time has elapsed since the start of the hydrotreating reaction of a feedstock containing a light oil fraction, and a calculation unit that calculates the deterioration levels of the desulfurization reaction and the cracking reaction of the catalyst using a deterioration function based on the information about the feedstock, information about the product oil, and information about the operating conditions acquired by the acquisition unit, calculates the information about the feedstock, information about the product oil, and information about the operating conditions based on the calculated deterioration level of the desulfurization reaction of the catalyst, calculates the reaction temperature required to satisfy the information about the feedstock, information about the product oil, and the operating conditions, and calculates the naphtha yield based on the calculated reaction temperature and the deterioration level of the cracking reaction of the catalyst.The naphtha yield calculation device of this embodiment may also have an output unit that outputs information about the calculated naphtha yield.

[0191] The hydrogen consumption calculation device 1 and naphtha yield calculation device 2 of this embodiment are configured using information processing devices such as a personal computer, a server device, or a dedicated device. The hydrogen consumption calculation device 1 and naphtha yield calculation device 2 may be configured using one or more information processing devices. Furthermore, the hydrogen consumption calculation device 1 and naphtha yield calculation device 2 may be configured using an integrated information processing device. For example, the hydrogen consumption calculation device 1 and naphtha yield calculation device 2 may be configured as a cluster machine, a cloud, or any other configuration. The hydrogen consumption calculation device 1 (naphtha yield calculation device 2) includes, for example, an acquisition unit 11 (acquisition unit 21) and a computer main body 12 (computer main body 22) that processes information from the acquisition unit, as shown in FIG. 3 (FIG. 4). The hydrogen consumption calculation device 1 (naphtha yield calculation device 2) may also include an output unit 14 (output unit 24) that outputs information processed in the computer main body 12 (computer main body 22) to the outside. These components are realized by, for example, a hardware processor such as a CPU (Central Processing Unit) executing a program (software). Furthermore, some or all of these components may be realized by hardware (including circuitry) such as an LSI (Large Scale Integrated circuit), an ASIC (Application Specific Integrated Circuit), an FPGA (Field-Programmable Gate Array), or a GPU (Graphics Processing Unit), or may be realized by a combination of software and hardware. The program may be stored in advance in a storage device (a storage device having a non-transitory storage medium) such as an HDD (Hard Disk Drive) or flash memory, or may be stored in a removable storage medium (a non-transitory storage medium) such as a DVD or CD-ROM, and installed in the storage device by inserting the storage medium into a drive device.The storage device may be configured, for example, by a HDD, a flash memory, an EEPROM (Electrically Erasable Programmable Read Only Memory), a ROM (Read Only Memory), or a RAM (Random Access Memory).

[0192] The acquisition unit 11 (acquisition unit 21) receives predetermined information input by a reaction operator and transmits the information acquired through this input to the computer main body 12. The acquisition unit 11 may also acquire information calculated by a naphtha yield calculation device, etc. The information acquired by the acquisition unit 11 of this embodiment is information about the feedstock oil over a certain period of time and information about the product oil, regarding the hydrotreating reaction of feedstock oil containing a light oil fraction. The information about the feedstock oil over a certain period of time and information about the product oil are as described above. For example, the acquisition unit 11 executes the information acquisition step described above. The acquisition unit 11 only needs to acquire information about the feedstock oil over a certain period of time and information about the product oil, and the acquisition method is not particularly limited. The information acquired by the acquisition unit 21 of this embodiment is information about the feedstock oil after a certain time has elapsed since the start of the reaction, information about the product oil, and information about the operating conditions, regarding the hydrotreating reaction of feedstock oil containing a light oil fraction. The information about the feedstock oil after a certain time has elapsed since the start of the reaction, information about the product oil, and information about the operating conditions are as described above. For example, the acquisition unit 21 executes the information acquisition step of the above-described information processing method A. The acquisition unit 21 only needs to acquire information on the feedstock oil, information on the product oil, and information on the operating conditions after a predetermined time has elapsed since the start of the reaction, and the acquisition method is not particularly limited.

[0193] In this embodiment, the acquisition unit 11 (acquisition unit 21) is configured with a single keyboard. The specific configuration of the acquisition unit 11 (acquisition unit 21) is not limited, and although it is a keyboard in this embodiment, it may also be a touch panel or the like. Note that acquisition units that acquire various types of information may be configured separately, and each may be independently connected to the computer main body 12 (computer main body 22). Furthermore, the acquisition unit 11 (acquisition unit 21) may be configured to directly acquire each piece of information from a computer or the like used for controlling a reactor, etc., via a wired or wireless connection. The acquisition unit 11 may also be configured to directly acquire each piece of information from the computer main body 22 via a wired or wireless connection.

[0194] The computer main body 12 (computer main body 22) is, for example, a so-called computer capable of processing various types of information. The computer main body 12 (computer main body 22) is equipped with an arithmetic unit 13 (arithmetic unit 23). For example, a predetermined program is installed in this computer main body 12 (computer main body 22), and the arithmetic unit 13 (arithmetic unit 23) is functionally configured by executing this program. Specifically, this arithmetic unit 13 calculates the amount of hydrogen consumed in the hydrotreating reaction during a certain period of time based on information regarding the feedstock oil and information regarding the product oil acquired by the acquisition unit 11. As described above, the amount of hydrogen can be determined, for example, from the hydrogen consumption function described above. Furthermore, the calculation unit 23 calculates the catalyst degradation level using a degradation function based on the information on the feedstock oil, the information on the product oil, and the information on the operating conditions acquired by the acquisition unit 21 at a predetermined time after the start of the reaction. The calculation unit 23 calculates the reaction temperature required to satisfy the information on the feedstock oil, the information on the product oil, and the operating conditions based on the catalyst degradation level, and calculates the naphtha yield based on the reaction temperature and the catalyst degradation level. The degradation function is as described above. As described above, the reaction temperature can be determined, for example, from a degradation rate equation. The naphtha yield can be determined, for example, from a naphtha yield function. The calculation unit 13 (calculation unit 23) may include, for example, a processor such as a CPU (Central Processing Unit) or an MPU (Micro Processing Unit), and non-volatile or volatile semiconductor memory (for example, RAM (Random Access Memory), ROM (Read Only Memory), flash memory, EPROM (Erasable Programmable Read Only Memory), or EEPROM (Electrically Erasable Programmable Read Only Memory)). For example, the calculation unit 13 (calculation unit 23) may be a microcontroller such as an MCU.

[0195] The calculation unit 13 may output information indicating the amount of hydrogen consumed in the hydrotreating reaction calculated as above to the output unit 14. The calculation unit 23 may output information indicating the amount of naphtha obtained as above to the output unit 24.

[0196] The output unit 14 (output unit 24) receives the calculation results (such as the amount of hydrogen consumed in the hydrotreating reaction and the amount of naphtha obtained) output by the computer main body 12 (computer main body 22) (more specifically, the calculation unit 13 (calculation unit 23)), and outputs the received calculation results to the outside. The output unit 14 (output unit 24) of this embodiment is configured by a display unit such as a CRT display, a liquid crystal display, or a PDP, but is not limited to these and may be configured to output to a printing unit such as a printer, or to other devices (for example, a computer used to control the hydrotreating reaction of diesel), etc. Furthermore, the output unit 14 (output unit 24) may be a combination of these. For example, the output unit 14 (output unit 24) executes the information output step described above.

[0197] Furthermore, in this embodiment, there is provided a hydrogen consumption amount calculation program or a naphtha yield calculation program for causing a computer to function as a hydrogen consumption amount calculation device or a naphtha yield calculation device, and a non-transitory computer-readable recording medium storing the program. Examples of non-transitory computer-readable recording media include magnetic tapes (such as digital data storage (DSS)), magnetic disks (such as hard disk drives (HDDs) and flexible disks (FDs)), optical disks (such as compact disks (CDs), digital versatile disks (DVDs), and Blu-ray disks (BDs)), magneto-optical disks (MOs), and flash memories (such as solid-state drives (SSDs), memory cards, and USB memories).

[0198] <Method of using information processing method and naphtha yield calculation device> According to the information processing method and naphtha yield calculation device of this embodiment, it is possible to estimate the amount of hydrogen consumed in the hydrotreating reaction of feedstock oil containing a light oil fraction. [Example]

[0199] The present invention will be explained in more detail below with reference to examples, but the present invention is not limited to the following examples.

[0200] [Analysis of the composition of feedstock oil and produced oil] The sulfur concentrations in the feedstock and the product oil were obtained by wavelength dispersive X-ray fluorescence spectroscopy. The naphtha concentration in the feedstock oil and the product oil was calculated from the proportion of fractions below 175°C in a distillation test. The concentrations of aromatic compounds in the feedstock and the product oil were obtained by high performance liquid chromatography (HPLC).

[0201] [Actual hydrogen consumption] As described above, the amount of make-up hydrogen was measured with a flow meter, and the measured value was taken as the actual hydrogen consumption amount.

[0202] [Feedstock supply volume] The feed oil supply rate was controlled by a feed oil delivery pump. [Example 1] Hydrotreating reaction was carried out by contacting feed oil containing diesel fraction with a hydrotreating catalyst. The composition of the feed oil and the product oil was analyzed over time. The results are shown in Table 1. The actual measured values ​​of hydrogen consumption (H RC ) divided by the feed oil supply amount (L) ((H RC ) / L) are also shown in Table 1. The actual hydrogen consumption and feed oil supply rates were measured using the methods described above. Data No. 1 represents data for a one-day (24-hour) period on the fourth day of operation, Data No. 2 represents data for a one-day (24-hour) period on the eighth day of operation, and so on. Measurements were made once per day, and the values ​​were taken as the average for that day. Using all the results from data 1 to 10, the Y axis is the hydrogen consumption amount and the X axis is a1(S F -S P )+a2(NA P -NA F )+a3(AR F -AR P) and performed multivariate analysis (with the intercept set to 0) to determine a1, a2, and a3 in the above formula 1. The results were a1 = 32.14, a2 = 0.36, and a3 = 2.96.

[0203] The obtained a1, a2, a3 and (S F -S P ), (NA P -NA F ), (AR F -AR P ) and the results of data 1 to 20 from Equation 1, the hydrogen consumption (H C ) divided by the feed oil supply amount (L) ((H C ) / L) was calculated. The results are shown in Table 2. As in Table 1, Data No. 1 represents data for a one-day (24-hour) period on the fourth day of operation, Data No. 2 represents data for a one-day (24-hour) period on the eighth day of operation, and so on.

[0204] [Table 1]

[0205] [Table 2]

[0206] As shown in Table 2, it was found that the hydrogen consumption amount determined by the present invention was almost the same as the actually measured value of the hydrogen consumption amount. [Explanation of symbols]

[0207] 1. Hydrogen consumption calculation device 11...Acquisition part 12...Calculator body 13... Arithmetic section 14. Output section 2. Naphtha yield calculation device 21...Acquisition part 22...calculator body 23... Arithmetic section 24 Output section

Claims

1. an information acquisition step of acquiring information about the feedstock and information about the product oil for a certain period of time regarding the hydrotreating reaction of the feedstock containing the light oil fraction; and a hydrogen amount calculation step of calculating the amount of hydrogen consumed in the hydrotreating reaction during the certain period based on the acquired information on the feedstock oil and information on the product oil, the information about the feedstock oil includes information about the density of the feedstock oil, information about the composition of the feedstock oil, and information about the feedstock oil supply amount, and the information about the product oil includes information about the density of the product oil and information about the composition of the product oil; the hydrotreating reaction includes a hydrodesulfurization reaction, a hydrocracking reaction, and a hydrogenation reaction, and the hydrogen amount calculating step is a step of calculating the amounts of hydrogen consumed in the hydrodesulfurization reaction, the hydrocracking reaction, and the hydrogenation reaction during the certain period of time; The amount of hydrogen consumed in the hydrogenation reaction is calculated based on information about the density of the feedstock oil and information about the density of the product oil; The information on the composition of the feedstock oil includes information on the sulfur concentration in the feedstock oil and information on the naphtha concentration in the feedstock oil, and the information on the composition of the product oil includes information on the sulfur concentration in the product oil and information on the naphtha concentration in the product oil, The information processing method, wherein the hydrogen amount calculation step is a step of calculating the hydrogen amount using a hydrogen consumption amount calculation function expressed by the following equation 3: [Equation 1] In Equation 3, H C is the estimated hydrogen consumption amount consumed in a certain period of time, S F(ave) is the average sulfur concentration in the feed oil for the certain period of time, S P(ave) is the average sulfur concentration in the product oil for the certain period of time, N A P(ave) is the average naphtha concentration in the product oil for the certain period of time, N A F(ave) is the average naphtha concentration in the feed oil for the certain period of time, DE F(ave) is the average density of the feed oil for the certain period of time, DE P(ave) is the average density of the product oil for the certain period of time, L is the feed amount of the feed oil for the certain period of time, and b 1 , b 2 , and b 3 are tuning factors that are constants greater than 0.

2. An information acquisition step for acquiring information about feedstock oil and information about product oil over a certain period of time regarding a hydrotreating reaction of feedstock oil containing a light oil fraction; and a hydrogen amount calculation step of calculating the amount of hydrogen consumed in the hydrotreating reaction during the certain period based on the acquired information on the feedstock oil and information on the product oil, the information about the feedstock oil includes information about the density of the feedstock oil, information about the composition of the feedstock oil, and information about the feedstock oil supply amount, and the information about the product oil includes information about the density of the product oil and information about the composition of the product oil; the hydrotreating reaction includes a hydrodesulfurization reaction, a hydrocracking reaction, and a hydrogenation reaction, and the hydrogen amount calculating step is a step of calculating the amounts of hydrogen consumed in the hydrodesulfurization reaction, the hydrocracking reaction, and the hydrogenation reaction during the certain period of time; The amount of hydrogen consumed in the hydrogenation reaction is calculated based on information about the density of the feedstock oil and information about the density of the product oil; The information on the composition of the feedstock oil includes information on the sulfur concentration in the feedstock oil and information on the naphtha concentration in the feedstock oil, and the information on the composition of the product oil includes information on the sulfur concentration in the product oil and information on the naphtha concentration in the product oil, An information processing method, wherein the information regarding the density of the produced oil is information obtained from information regarding the density of the feedstock oil, and the hydrogen amount calculation step is a step of calculating the hydrogen amount using a hydrogen consumption amount calculation function expressed by the following equation 4. [Equation 2] In the formula 4, H Ｃ is the estimated hydrogen consumption amount consumed in a certain period of time, and S Ｆ（ａｖｅ） is the average sulfur concentration in the feed oil for the given period, and S Ｐ（ａｖｅ） is the average sulfur concentration in the produced oil for the given period, and NA Ｐ（ａｖｅ） is the average naphtha concentration in the produced oil for the given period, and NA Ｆ（ａｖｅ） is the average naphtha concentration in the feedstock oil for the given period, and DE Ｆ（ａｖｅ） is the average density of the feedstock oil for the given period, and DE Ｐ（ａｖｅ） ' is the estimated average density of the produced oil for the certain period calculated by the following formula 5, and f Ｈ is a tuning factor, a constant, L is the feed oil supply amount for the given period, and b １ , b ２ , b ３ is a tuning factor, a constant greater than zero. [Equation 3] In the formula 5, DE Ｆ（ａｖｅ） is the average density of the feedstock oil for the certain period, T is the average reaction temperature (°C) for the certain period, and α, β, and σ are catalyst coefficients determined for each catalyst used and are constants.

3. an information acquisition step of acquiring information about the feedstock and information about the product oil for a certain period of time regarding the hydrotreating reaction of the feedstock containing the light oil fraction; and a hydrogen amount calculation step of calculating the amount of hydrogen consumed in the hydrotreating reaction during the certain period based on the acquired information on the feedstock oil and information on the product oil, The information processing method, wherein the hydrogen amount calculation step is a step of calculating the hydrogen amount using a hydrogen consumption amount calculation function expressed by the following equation 1: [Equation 4] In the formula 1, H Ｃ is the estimated hydrogen consumption amount consumed in a certain period of time, and S Ｆ（ａｖｅ） is the average sulfur concentration in the feed oil for the given period, and S Ｐ（ａｖｅ） is the average sulfur concentration in the produced oil for the given period, and NA Ｐ（ａｖｅ） is the average naphtha concentration in the produced oil for the given period, and NA Ｆ（ａｖｅ） is the average naphtha concentration in the feedstock oil for the given period, and AR Ｆ（ａｖｅ） is the average aromatic compound concentration in the feedstock for the given period, and AR Ｐ（ａｖｅ） is the average aromatic compound concentration in the produced oil for the given period, L is the feed oil supply amount for the given period, and a １ , a ２ , a ３ is a tuning factor, a constant greater than zero.

4. A hydrogen consumption calculation device comprising: an acquisition unit that acquires information about a feedstock oil and information about a product oil for a certain period of time in relation to a hydrotreating reaction of a feedstock oil containing a light oil fraction; and a calculation unit that calculates an amount of hydrogen consumed in the hydrotreating reaction for the certain period of time based on the information about the feedstock oil and the information about the product oil acquired by the acquisition unit, the information about the feedstock oil includes information about the density of the feedstock oil, information about the composition of the feedstock oil, and information about the feedstock oil supply amount, and the information about the product oil includes information about the density of the product oil and information about the composition of the product oil; the hydrotreating reaction includes a hydrodesulfurization reaction, a hydrocracking reaction, and a hydrogenation reaction, and the calculation of the amount of hydrogen is performed by calculating the amounts of hydrogen consumed in the hydrodesulfurization reaction, the hydrocracking reaction, and the hydrogenation reaction during the certain period of time; The amount of hydrogen consumed in the hydrogenation reaction is calculated based on information about the density of the feedstock oil and information about the density of the product oil; The information on the composition of the feedstock oil includes information on the sulfur concentration in the feedstock oil and information on the naphtha concentration in the feedstock oil, and the information on the composition of the product oil includes information on the sulfur concentration in the product oil and information on the naphtha concentration in the product oil, The hydrogen consumption calculation device calculates the amount of hydrogen using a hydrogen consumption calculation function expressed by the following equation 3. [Equation 5] In Equation 3, H C is the estimated hydrogen consumption amount consumed in a certain period of time, S F(ave) is the average sulfur concentration in the feed oil for the certain period of time, S P(ave) is the average sulfur concentration in the product oil for the certain period of time, N A P(ave) is the average naphtha concentration in the product oil for the certain period of time, N A F(ave) is the average naphtha concentration in the feed oil for the certain period of time, DE F(ave) is the average density of the feed oil for the certain period of time, DE P(ave) is the average density of the product oil for the certain period of time, L is the feed amount of the feed oil for the certain period of time, and b 1 , b 2 , and b 3 are tuning factors that are constants greater than 0.

5. A hydrogen consumption calculation device comprising: an acquisition unit that acquires information about feedstock oil and information about product oil over a certain period of time in relation to a hydrotreating reaction of feedstock oil containing a light oil fraction; and a calculation unit that calculates the amount of hydrogen consumed in the hydrotreating reaction over the certain period of time based on the information about the feedstock oil and the information about the product oil acquired by the acquisition unit, the information about the feedstock oil includes information about the density of the feedstock oil, information about the composition of the feedstock oil, and information about the feedstock oil supply amount, and the information about the product oil includes information about the density of the product oil and information about the composition of the product oil; the hydrotreating reaction includes a hydrodesulfurization reaction, a hydrocracking reaction, and a hydrogenation reaction, and the calculation of the amount of hydrogen is performed by calculating the amounts of hydrogen consumed in the hydrodesulfurization reaction, the hydrocracking reaction, and the hydrogenation reaction during the certain period of time; The amount of hydrogen consumed in the hydrogenation reaction is calculated based on information about the density of the feedstock oil and information about the density of the product oil; The information on the composition of the feedstock oil includes information on the sulfur concentration in the feedstock oil and information on the naphtha concentration in the feedstock oil, and the information on the composition of the product oil includes information on the sulfur concentration in the product oil and information on the naphtha concentration in the product oil, A hydrogen consumption calculation device, wherein the information about the density of the product oil is information obtained from information about the density of the feedstock oil, and the calculation of the amount of hydrogen is performed using a hydrogen consumption calculation function expressed by the following equation 4. [Equation 6] In the formula 4, H Ｃ is the estimated hydrogen consumption amount consumed in a certain period of time, and S Ｆ（ａｖｅ） is the average sulfur concentration in the feed oil for the given period, and S Ｐ（ａｖｅ） is the average sulfur concentration in the produced oil for the given period, and NA Ｐ（ａｖｅ） is the average naphtha concentration in the produced oil for the given period, and NA Ｆ（ａｖｅ） is the average naphtha concentration in the feedstock oil for the given period, and DE Ｆ（ａｖｅ） is the average density of the feedstock oil for the given period, and DE Ｐ（ａｖｅ） ' is the estimated average density of the produced oil for the certain period calculated by the following formula 5, and f Ｈ is a tuning factor, a constant, L is the feed oil supply amount for the given period, and b １ , b ２ , b ３ is a tuning factor, a constant greater than zero. [Equation 7] In the formula 5, DE Ｆ（ａｖｅ） is the average density of the feedstock oil for the certain period, T is the average reaction temperature (°C) for the certain period, and α, β, and σ are catalyst coefficients determined for each catalyst used and are constants.

6. A hydrogen consumption calculation device comprising: an acquisition unit that acquires information about a feedstock oil and information about a product oil over a certain period of time in relation to a hydrotreating reaction of a feedstock oil containing a light oil fraction; and a calculation unit that calculates an amount of hydrogen consumed in the hydrotreating reaction over the certain period of time based on the information about the feedstock oil and the information about the product oil acquired by the acquisition unit, wherein the calculation of the amount of hydrogen is performed using a hydrogen consumption calculation function expressed by the following equation 1. [Equation 8] In the formula 1, H Ｃ is the estimated hydrogen consumption amount consumed in a certain period of time, and S Ｆ（ａｖｅ） is the average sulfur concentration in the feed oil for the given period, and S Ｐ（ａｖｅ） is the average sulfur concentration in the produced oil for the given period, and NA Ｐ（ａｖｅ） is the average naphtha concentration in the produced oil for the given period, and NA Ｆ（ａｖｅ） is the average naphtha concentration in the feedstock oil for the given period, and AR Ｆ（ａｖｅ） is the average aromatic compound concentration in the feedstock for the given period, and AR Ｐ（ａｖｅ） is the average aromatic compound concentration in the produced oil for the given period, L is the feed oil supply amount for the given period, and a １ , a ２ , a ３ is a tuning factor, a constant greater than zero.

7. A hydrogen consumption calculation program for causing a computer to function as the hydrogen consumption calculation device according to any one of claims 4 to 6.

8. A non-transitory computer-readable recording medium storing the program according to claim 7.

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