JP7716211B2 - Information processing method, reaction temperature calculation device, reaction temperature calculation program, and non-transitory computer-readable recording medium - Google Patents

Description

The present invention relates to an information processing method, a reaction temperature calculation device, a reaction temperature calculation program, and a non-transitory computer-readable recording medium.

Atmospheric residue oil, obtained by atmospheric distillation of crude oil, contains a high concentration of sulfur. The method of reducing the sulfur content of atmospheric residue oil by hydrotreating it is known as direct desulfurization. On the other hand, the method of reducing the sulfur content of atmospheric residue oil by vacuum distillation, separating it into vacuum gas oil and vacuum residue oil, hydrotreating the vacuum gas oil to reduce the sulfur content, and then blending the hydrotreated vacuum gas oil with the vacuum residue is known as indirect desulfurization.

During the hydrotreatment of vacuum distillation gas oil, coke is produced as a by-product, and as the coke accumulates on the hydrotreatment catalyst, the activity of the hydrotreatment catalyst decreases over time. Therefore, in order to keep the sulfur content in the resulting oil below a certain level, the reaction temperature must be increased to counteract the decrease in activity of the hydrotreatment catalyst.

When setting this reaction temperature, if the reaction temperature is too high, the catalyst's activity will decline, making it impossible to achieve the specified operating time (number of days), resulting in reduced productivity. On the other hand, if the reaction temperature is too low, the catalyst's activity will decline less, resulting in excess capacity before the specified operating time is reached, and productivity will decrease if this excess capacity cannot be utilized. Therefore, a method for accurately estimating specified reaction conditions (temperature, throughput) is desired.

In the field of crude oil refining, various methods for accurately estimating the optimal reaction temperature have been studied. For example, Patent Document 1 discloses a method for estimating the reaction temperature required after switching from atmospheric distillation gas oil to another feedstock containing atmospheric distillation gas oil with different properties in the hydroprocessing of the feedstock, based on information about the properties of the atmospheric distillation gas oil before the switch and the operating conditions, and information about the properties of the atmospheric distillation gas oil after the switch and the operating conditions other than the reaction temperature.

Japanese Patent Application Publication No. 10-60455

The method for estimating the reaction temperature described in Patent Document 1 focuses on the properties of the feedstock oil, and does not consider the reduction in activity of the hydrotreating catalyst. Therefore, there is a need for a method for estimating the optimal reaction temperature while taking into account the reduction in activity of the hydrotreating catalyst.

The present invention was made in consideration of the above circumstances, and aims to provide an information processing method capable of estimating the reaction temperature required to achieve specified reaction conditions for the hydrotreating reaction of feedstock oil, including vacuum distillation gas oil; a reaction temperature calculation device capable of estimating the reaction temperature; a reaction temperature calculation program for causing a computer to function as the reaction temperature calculation device; and a non-transitory computer-readable recording medium storing the program.

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 vacuum distillation gas oil obtained by vacuum distillation of atmospheric distillation residual oil, comprising: an information acquisition step for acquiring information on the feedstock, information on the product oil, and information on operating conditions at a predetermined time after the start of the reaction; a degradation degree calculation step for calculating a catalyst degradation level using a degradation function based on the acquired information on the feedstock, information on the product oil, and information on the operating conditions; and a reaction temperature calculation step for calculating a reaction temperature required to satisfy the information on the feedstock, information on the product oil, and the operating conditions based on the catalyst degradation level.
[2] The deterioration function is a coke deterioration function relating to catalyst deterioration due to coke deposition, and is composed of an easily deactivated active species deterioration function relating to the deterioration of easily deactivated active species of the catalyst and a hardly deactivated active species deterioration function relating to the deterioration of hardly deactivated active species of the catalyst. The information processing method described in [1].
[3] The information processing method according to [1] or [2], wherein the information about the feedstock oil includes information about the sulfur concentration in the feedstock oil, and the information about the product oil includes information about the sulfur concentration in the product oil.
[4] The information processing method according to any one of [1] to [3], wherein the information about the operating conditions includes information about hydrogen partial pressure, information about catalyst loading, and information about the feedstock supply amount.
[5] A reaction temperature calculation device including: an acquisition unit that acquires information about the feedstock oil, information about the product oil, and information about the operating conditions at a predetermined time after the start of the reaction, regarding the hydrotreating reaction of the feedstock oil including vacuum distillation gas oil obtained by vacuum distillation of atmospheric distillation residual oil; and a calculation unit that calculates the degree of catalyst deterioration using a deterioration function based on the information about the feedstock oil, the information about the product oil, and the information about the operating conditions acquired by the acquisition unit, and calculates the reaction temperature required to satisfy the information about the feedstock oil, the information about the product oil, and the operating conditions based on the calculated degree of catalyst deterioration.
[6] The deterioration function is a coke deterioration function relating to catalyst deterioration due to coke deposition, and is composed of an easily deactivated active species deterioration function relating to deterioration of easily deactivated active species of the catalyst and a hardly deactivated active species deterioration function relating to deterioration of hardly deactivated active species of the catalyst. The reaction temperature calculation device described in [5].
[7] The information about the feedstock oil includes information about the sulfur concentration in the feedstock oil, and the information about the product oil includes information about the sulfur concentration in the product oil. The reaction temperature calculation device according to [5] or [6].
[8] The reaction temperature calculation device according to any one of [5] to [7], wherein the information on the operating conditions includes information on hydrogen partial pressure, information on catalyst loading, and information on the feedstock supply amount.
[9] A reaction temperature calculation program for causing a computer to function as the reaction temperature calculation device according to any one of [5] to [8].
[10] A non-transitory computer-readable recording medium storing the program according to [9].

The present invention provides an information processing method capable of estimating the reaction temperature required to achieve specified reaction conditions for the hydrotreating reaction of feedstock oil, including vacuum distillation gas oil, a reaction temperature calculation device capable of estimating the reaction temperature, a reaction temperature calculation program for causing a computer to function as the reaction temperature calculation device, and a non-transitory computer-readable recording medium storing the program.

1 is a flowchart of an information processing method according to an embodiment. 1 is a flowchart of an information processing method according to an embodiment. 1 is a flowchart of an information processing method according to an embodiment. FIG. 1 is a configuration block diagram of a reaction temperature calculation device according to an embodiment.

The following describes in detail the embodiments of the present invention. However, the following description is merely an example of an embodiment of the present invention, and the present invention is not limited to these details and can be modified and implemented within the scope of its essence.

<Information processing method>
The information processing method of this embodiment relates to a hydrotreating reaction of a feedstock containing vacuum distillation gas oil obtained by vacuum distillation of atmospheric distillation residue oil. The method includes an information acquisition step (S1 in FIG. 1) for acquiring information on the feedstock, information on the product oil, and information on operating conditions at a predetermined time after the start of the reaction; a deterioration degree calculation step (S2 in FIG. 1) for calculating the deterioration level of the catalyst using a deterioration function based on the acquired information on the feedstock, information on the product oil, and information on the operating conditions; and a reaction temperature calculation step (S3 in FIG. 1) for calculating the reaction temperature required to satisfy the information on the feedstock, information on the product oil, and the operating conditions based on the deterioration level of the catalyst. Each step will be described below. Note that each step shown below is executed, for example, by the reaction temperature calculation device 1 of this embodiment. For example, S1 is executed by the acquisition unit 11, and S2 and S3 are executed by the calculation unit 13 in the computer main body 12.

<Information Acquisition Steps>
The information acquisition step of this embodiment is a step of acquiring information about the feedstock oil, information about the product oil, and information about the operating conditions when a predetermined time has elapsed since the start of the reaction. The predetermined time after the start of the reaction refers to, for example, any t days having elapsed since the start of the reaction. t may be an integer or a decimal; for example, if t is 0.5, it means that 12 hours have elapsed since the start of the reaction. Furthermore, the time when t days have elapsed may be in the past, present, or future from the time when the information processing method of this embodiment is implemented. For example, if the information processing method of this embodiment is implemented two days after the start of the reaction and t is 4, the reaction temperature two days later (in the future) will be estimated.

(Information about feedstock oil)
An example of the information about the feedstock oil is information about the composition of the feedstock oil. An example of the information about the composition of the feedstock oil is information about the sulfur concentration in the feedstock oil.

Information regarding the sulfur concentration in the feedstock oil can be obtained using sulfur concentration measurement methods known in the art, such as ultraviolet fluorescence spectroscopy and wavelength-dispersive X-ray fluorescence spectroscopy. The sulfur concentration in the feedstock oil can also be controlled by changing the feedstock oil. It is preferable that the information regarding the sulfur concentration in the feedstock oil is a set value. In other words, the sulfur concentration of the feedstock oil planned for use can be used.

(Information about produced oil)
Examples of the information about the product oil include information about the composition of the product oil, and information about the sulfur concentration in the product oil.

Information regarding the sulfur concentration in the product oil can be obtained in the same manner as in the case of the feedstock oil described above. In this embodiment, the information regarding the sulfur concentration in the product oil is preferably a set value. In other words, the sulfur concentration of the target product oil can be used.

(Information about operating conditions)
Examples of information about operating conditions include information about hydrogen partial pressure, information about catalyst loading, information about the feedstock feed rate, and information about the hydrogen feed rate. For example, the information about operating conditions is at least one of information about hydrogen partial pressure, information about catalyst loading, information about the feedstock feed rate, and information about the hydrogen feed rate. In particular, the information about operating conditions preferably includes information about hydrogen partial pressure, information about catalyst loading, and information about the feedstock feed rate, and more preferably includes all of information about hydrogen partial pressure, information about catalyst loading, information about the feedstock feed rate, and information about the hydrogen feed rate. The operating conditions also include time information, such as the elapse of any t days since the start of the reaction.

Information regarding hydrogen partial pressure, catalyst loading, feedstock feed rate, and hydrogen feed rate can be determined by methods known in the art. Information regarding hydrogen partial pressure, catalyst loading, feedstock feed rate, and hydrogen feed rate can be controlled in the hydrotreating reaction of feedstocks, including vacuum distillation gas oil. Information regarding operating conditions is preferably a set value; that is, the planned operating conditions are used.

<Deterioration level calculation step>
The deterioration level calculation step of this embodiment is a step of calculating the deterioration level of the catalyst using a deterioration function based on the acquired information on the feedstock oil, information on the refined oil, and information on the operating conditions.

<Degree of deterioration>
The degree of deterioration is expressed by the following formula 1.
Φ=k _t /k ₀ Equation 1
In the above formula 1, _k0 is the reaction rate constant of the catalyst after 0 days of reaction (i.e., at the start of the reaction), and _kt is the reaction rate constant of the catalyst after t days of reaction. Note that _k0 and _kt are reaction rate constants at a temperature T _SOR described below.

In this embodiment, the degree of catalyst degradation can be calculated using a degradation function based on the acquired information about the feedstock oil, information about the product oil, and information about the operating conditions.

<Deterioration function 1>
The deterioration function is a function for calculating the deterioration level of the catalyst. In this embodiment, the deterioration function is preferably a coke deterioration function relating to catalyst deterioration 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 relating to coke deterioration of the catalyst. For example, deterioration function 1 expressed by the following formula 2 can be given as an example.

Φ=exp(-Dt) Formula 2
In the above formula 2, D is the deterioration coefficient of the active species of the catalyst, and t is the number of days elapsed since the reaction began.

D can be calculated using the following equation 3. Equation 3 below is a formula that can calculate the deterioration coefficient of the catalyst's active species using specific parameters, and was first discovered by the inventors of this application based on the operating results of actual equipment.

In the above formula 3, α is a catalyst constant (a constant representing the rate of catalyst deterioration), S _F is the sulfur concentration (mass%) in the feedstock oil after t days of reaction, 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 vacuum distillation gas oil, LHSV is the liquid hourly space velocity (h ^-1 ) after t days of reaction, P _B is the reference hydrogen partial pressure (MPa), P is the hydrogen partial pressure (MPa) after t days of reaction, a is the hydrogen partial pressure coefficient, Ec is the activation energy of coke deterioration (kJ / mol), R is a gas constant: 0.00831 (kJ / (mol · K)), T _B is the reference reaction temperature (K), and T _SOR is the required temperature on day 0 (K).

As used herein, the term "required temperature" refers to the reaction temperature required to achieve predetermined reaction conditions. That is, the required temperature on day 0 refers to the reaction temperature required to achieve the above-mentioned reaction conditions of S _F , S _P , LHSV, and P at the start of the reaction.

In this specification, "reference hydrogen partial pressure" refers to the standard pressure under actual reaction conditions. It is calculated as the average reaction pressure used when determining the hydrogen partial pressure coefficient a, which will be described later.

In this specification, the "reference reaction temperature" means the average value of T _SOR obtained over a range of standard operating conditions that may be actually encountered during operation.

In Equation 3, T _SOR represents the initial activity of the catalyst, and α represents the rate of catalyst deterioration. That is, the larger the values of T _SOR and α, the greater the catalyst deterioration, and this deterioration behavior is reflected in the value of D.

In the above equation 3, the term expressed by (1/S _P ^n-1 -1/S _F ^n-1 )LHSV is a desulfurization reaction rate constant, and as described above, is a constant when S _P , S _F , and LHSV are set values and operation is performed under constant conditions. In the above equation 3, the term expressed by (P _B /P) ^a is a term indicating hydrogen partial pressure dependency, and as described above, is a constant when P is set value and operation is performed under constant conditions. In the above equation 3, the term expressed by exp[Ec/R(1/T _B -1/T _SOR )] is a term indicating temperature dependency and is a constant.

In the above formula 3, S _F , S _P , LHSV, and P 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 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).

As described above, S _F , LHSV, and P are controllable parameters. Furthermore, S _P is the sulfur concentration of the target product oil. That is, the deterioration coefficient of the active species of the catalyst under the reaction conditions of S _F , S _P , LHSV, and P can be calculated using Equation 3. The method for determining n, which is the reaction order of the hydrotreating reaction of feedstock oil containing vacuum distillation gas oil, will be described later.

(How to determine basic degradation parameters)
In the above formula 3, α, P _B , a, Ec, T _B , and T _SOR are constants. 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 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 the parameter in advance on a bench scale based on the operating conditions of the actual machine.
Below, examples of how to determine the basic deterioration parameters P _B , a, Ec, and T _B are shown. These methods (methods for determining P _B , a, Ec, and T _B ) are based on the catalyst deterioration behavior (changes in reaction rate constants) analyzed from data obtained from the above-mentioned reaction on an actual plant or a bench-scale reaction under actual plant operating conditions. Two examples of how to determine α and T _SOR are shown, but the present invention is not limited to these. The first example is a method (method 1 for determining α and T SOR) in which the parameters are determined from the catalyst deterioration behavior (changes in reaction rate constants) analyzed from data obtained from the above-mentioned reaction on an actual plant or a bench-scale reaction under actual plant operating conditions. The second example is a method (method 2 for determining α and T _SOR ) in which the parameters are determined from the reaction temperature profile analyzed from data obtained from the above-mentioned reaction on an actual plant or a bench-scale reaction under actual _plant operating conditions.

(How to calculate P _B , a, Ec, and T _B )
The method for determining the basic deterioration parameters in this embodiment is based on the deterioration behavior of the catalyst analyzed from data obtained from the above-mentioned reaction in an actual machine or a bench-scale reaction under actual machine operating conditions. This catalyst deterioration behavior (degree of deterioration) can be expressed by the following equation 4, based on the same concept as equation 1.
Φ'=k _t '/k ₀ ' Equation 4
In the above formula 4, k ₀ ' is the reaction rate constant 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 catalyst after t days of reaction. Note that k ₀ ' and k _t ' are reaction rate constants at a temperature T _SOR ' described below.

Equation 4, like equation 1, is a degradation function based on the reaction rate constant. The reaction rate constant is expressed by the Arrhenius equation in equation 5 below.

In the above formula 5, k is the reaction rate constant, A is the frequency factor, E is the activation energy (kJ/mol), R is the gas constant: 0.00831 (kJ/(mol·K)), and T is the reaction temperature (K).

The reaction rate constant k ₀ ' at the reaction start temperature T _SOR ' decreases to k _t ' after t days of reaction. If the reaction temperature must be set to T _t ' to obtain activity equivalent to the reaction rate constant k ₀ ' after t days of reaction, then the following equation 6 can be derived from equations 4 and 5. Note that since the reaction in this embodiment is a hydrotreating reaction of a feedstock oil containing vacuum distillation gas oil, the activation energy E is set to the desulfurization activation energy Ea (kJ/mol).

In this embodiment, P _B , a, Ec, and T _B are calculated based on the above-mentioned formula 6.

(How to calculate Ec and T _B )
The reaction is carried out for a certain period of time under constant conditions of LHSV, hydrogen partial pressure, hydrogen/feed oil ratio, and sulfur concentration in the feed oil so that the sulfur concentration in the product oil reaches a certain value _SPn . Because the catalyst deteriorates due to the reaction, operation is carried out while increasing the reaction temperature in order to maintain the sulfur concentration in the product oil at _SPn . By plotting the reaction time on the horizontal axis and the measured reaction temperature on the vertical axis and drawing a regression line, a straight line expressed as y = a _n x + b _n (0 < a _n ) is obtained. _{a n} and b _n are values reflecting the deterioration behavior of the catalyst. b _n in this straight line is T _SOR ' in the above formula 6. In the above formula 6, by substituting b _n for T _SOR ' and substituting the measured reaction temperature for T _t ', the deterioration degree Φ' after any reaction time t days has elapsed can be obtained. The desulfurization activation energy Ea can be determined using a value determined by the method described below. If we plot the reaction time on the horizontal axis and the logarithm of Φ' on the vertical axis and draw a regression line, we obtain a line expressed as y = -a _n ^' x (|-a _n ^' | = a _n ^' ), where _{a n} ^' represents the catalyst deterioration rate.

The same reaction is carried out for n types of sulfur concentration S _Pn , and n a _n and b _n are determined in the same manner, and n a _n ^' are obtained by the same method as above. n is an integer of 3 or more. The larger the number of n, the more accurate Ec can be obtained. On the other hand, if the number 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 _n ^'s and b _n values thus obtained are respectively substituted into the following formula 7. The following formula 7 is an equation that can calculate the activation energy and reference reaction temperature of coke, and was first discovered by the inventors of the present application based on the operating results of an actual machine, etc.

ln( _an ^' )=ln(A)-(Ec/ _Rbn ) Equation 7
In Equation 7, A is a frequency factor, Ec is the activation energy of coke deterioration (kJ/mol), and R is the gas constant: 0.00831 (kJ/(mol·K)).

For n combinations of a _n ^' and b _n , ln(a _n ^' ) is plotted 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.

Also, T _B can be obtained by averaging n b _n values.

In determining Ec and _TB , 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 an actual plant.
Such an LHSV is, for example, 0.5 to 2.5 h ⁻¹ , the hydrogen partial pressure is, for example, 3 to 7 MPa, the hydrogen/feed oil ratio is, for example, 100 to 400 [Nm ³ /kL], and the sulfur concentration in the feed oil is, for example, 0.5 to 3.0 mass %.
Similarly, it is preferable that the n-type sulfur concentrations S _Pn are set to conditions that correspond to the actual operating conditions of the engine, and such S _Pn is, for example, 0.3 mass % or less.
The reaction period is, for example, 100 to 1500 days.

(How to calculate P _B and a)
The reaction is carried out for a certain period of time under conditions of constant LHSV, hydrogen/feed oil ratio, sulfur concentration in the feed oil, and sulfur concentration in the product oil, and hydrogen partial pressure _Pm . Because the catalyst deteriorates due to the reaction, operation is carried out while increasing the reaction temperature in order to maintain a constant sulfur concentration in the product oil. When the reaction time is plotted on the horizontal axis and the measured reaction temperature on the vertical axis and a regression line is drawn, a straight line expressed as y = a _m x + b _m (0 < a _m ) is obtained. b _m on this line becomes T _SOR ' in the above-mentioned formula 6. When b _m is substituted for T _SOR ' in the above-mentioned formula 6 and the measured reaction temperature is substituted for T _t ', the deterioration degree Φ' after any reaction time of t days has elapsed can be obtained. When the reaction time is plotted on the horizontal axis and the logarithm of Φ' on the vertical axis and a regression line is drawn, a straight line expressed as y = -a _m ^' x (|-a _m ^' | = a _m ^' ) is obtained. a _m ^′ represents the catalyst deterioration rate.

The same reaction is carried out for m types of hydrogen partial pressure P _m , m a _m and b _m are determined in the same manner, and m a _m ^' are obtained by the same method as above. m is an integer of 3 or more. The larger the number of m, the more accurate a can be obtained. On the other hand, if the number 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 _m 's and P _m obtained in this way are respectively substituted into the following formula 8. The following formula 8 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.

ln( _am ^' )=-aln( _Pm )+B1 Equation 8
In the formula 8, B1 can be 0.

For m combinations of a _m ' and P _m , ln(a _m ^' ) is plotted on the vertical axis and ln(P _m ) on the horizontal axis, a regression line is drawn, and the slope is determined. This slope is the hydrogen partial pressure coefficient a.

Moreover, P _B can be obtained by averaging the m hydrogen partial pressures P _m .

In determining a and P _B , the LHSV, hydrogen/feed oil ratio, sulfur concentration in the feed oil, and sulfur concentration in the product oil are preferably set to conditions that correspond to the operating conditions of an actual plant.
Such an LHSV is, for example, 0.5 to 2.5 h ⁻¹ , the hydrogen/feed oil ratio is, for example, 100 to 400 [Nm ³ /kL], the sulfur concentration in the feed oil is, for example, 0.5 to 3.0 mass %, and the sulfur concentration in the product oil is, for example, 0.3 mass % or less.
Similarly, it is preferable that the partial pressure _Pm of the m types of hydrogen is set to a condition that corresponds to the operating conditions of the actual plant. For example, _Pm is 3 to 7 MPa. The reaction period is, for example, 50 to 600 days.

(Method 1 for determining α and T _SOR )
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 actual plant operating conditions. Because the catalyst deteriorates during the reaction, operation is carried out while increasing the reaction temperature. Examples of the assumed actual plant operating conditions include the operating conditions described in (How to determine Ec and T _B ) and (How to determine P _B and a). By plotting the reaction time on the horizontal axis and the measured reaction temperature on the vertical axis and drawing a regression line, a straight line expressed as y = a _α x + b _α is obtained. In this line, a _α is a value correlated with α in Equation 3, and b _α is T _SOR in Equation 3. Substituting b _α for T _SOR ' and the measured reaction temperature for T _t ' in Equation 6 gives the degree of deterioration Φ' after any reaction has elapsed t days. If we plot the reaction time on the horizontal axis and the logarithm of Φ' on the vertical axis and draw a regression line, we obtain a line expressed as y = -a _α ^' x (where |-a _α ^' | = a _α ^' ), where _{a α} ^' represents the catalyst deterioration rate.

D is determined by substituting the operating conditions S _P , S _F , LHSV, and P, and P _B , a, Ec, T _{B , and} T _SOR (i.e., b _α ) determined by the above method into Equation 3. Φ is obtained by substituting the determined D into Equation 2. 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 while changing α so that α is 0 < α, multiple straight lines expressed as y = -a _α ^" x (|-a _α ^" | = a _α ^" ) are obtained for each value of α. The α when a _α ^" on each straight line is equal to the above-mentioned a _α ^' can be defined as the α in Equation 3.

(Method 2 for determining α and T _SOR )
A reaction similar to that in (Method 1 for Determining α and T _SOR ) is carried out to obtain a straight line expressed by y = a _α x + b _α , and b _α is defined as T _SOR in the above formula 3. D is determined by substituting the operating conditions S _P , S _F , LHSV, and P, and P _B , a, Ec, T _{B , and} T _SOR (i.e., b _α ) determined by the above method into the above formula 3. Φ is obtained by substituting the determined D into the above formula 2. In this case, Φ is a function of α. By substituting the obtained Φ into Φ' in the above formula 6 and substituting T _SOR (i.e., b _α ) into T _SOR ^' in the above formula 6 and rearranging for T _t ', T _t ' becomes a function of α. α when the ratio of T _t ' to the measured reaction temperature T _obs (T _t '/T _obs ) becomes 1 can be defined as α in the above formula 3. Similarly, it is preferable to calculate the ratio of T _t ' to N reaction temperatures T _obs (T _t '/T _obs ), and define the α when the average of these is closest to 1 as the α in the above formula 3. N is an integer of 10 or more, preferably 10 to 500, and more preferably 50 to 200.

(Modification of degradation function 1)
The following describes a modification of the point spread function 1. As the point spread function 1, a point spread function 1-1 expressed by the following equation 9 may be used.

Φ=exp(-D't) Equation 9
In the above formula 9, D' is the deterioration coefficient of the active species of the catalyst, and t is the number of days elapsed since the reaction began.

D' can be calculated using the following formula 10.

In the above equation (10), α' is a catalyst constant (a constant representing the rate of catalyst deterioration), S _F is the sulfur concentration (mass%) in the feed oil after t days of reaction, 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 feed oil containing vacuum distillation gas oil, LHSV is the liquid hourly space velocity (h ^-1 ) after t days of reaction, P _B is the reference hydrogen partial pressure (MPa), P is the hydrogen partial pressure (MPa) after t days of reaction, a is the hydrogen partial pressure coefficient, G _B is the reference hydrogen/feed oil ratio (Nm ³ /kL), G is the hydrogen/feed oil ratio (Nm ³ /kL) after t days of reaction, b is the hydrogen/feed oil ratio coefficient, Ec is the activation energy of coke deterioration (kJ/mol), R is a gas constant: 0.00831 (kJ/(mol·K)), and T _B is the reference reaction temperature (K) and T _SOR is the required temperature on day 0 (K).

S _F , S _P , LHSV, and P in the above formula 10 are the same as those in the above formula 3. In the above formula 10, G is a value substituted based on the information on the feedstock oil and the information on the operating conditions acquired in the above-mentioned information acquisition step. Specifically, G can be calculated by dividing the hydrogen supply rate (Nm ³ /hour) by the feedstock oil supply rate (kL/hour).

In this specification, "reference hydrogen/feed oil ratio" refers to the standard hydrogen/feed oil ratio under actual reaction conditions. It is calculated as the average hydrogen/feed oil ratio used when determining the hydrogen/feed oil ratio coefficient b, which will be described later.

In the above formula 10, the term expressed by (G _B /G) ^b is a term that indicates dependency on the hydrogen/feed oil ratio, and as described above, becomes a constant when G is a set value and operation is performed under constant conditions.

P _B , a, Ec, T _B , and T _SOR can be calculated in the same manner as described above for Equation 3. How to calculate G _B , b, and α' will now be described.

_GB and b, like P _B , a, Ec, _TB and _TSOR, are parameters determined depending on the catalyst used, and may be determined while performing the reaction in an actual reaction system, or may be determined in advance on a bench scale based on the operating conditions of the actual reaction system. In this embodiment, it is preferable to determine them in advance on a bench scale based on the operating conditions of the actual reaction system. Hereinafter, how to determine _GB and b will be described.

(How to find _GB and b)
The method for determining the basic deterioration parameters in this embodiment is based on the deterioration behavior of the catalyst analyzed from data obtained from the above-mentioned reaction in the actual equipment or from a bench-scale reaction under the operating conditions of the actual equipment.

The reaction is carried out for a certain period of time under the conditions of constant LHSV, hydrogen partial pressure, sulfur concentration in the feed oil, and sulfur concentration in the product oil, and a hydrogen/feed oil ratio of G _h . Because the catalyst deteriorates due to the reaction, operation is carried out while increasing the reaction temperature in order to maintain a constant sulfur concentration in the product oil. When the reaction time is plotted on the horizontal axis and the measured reaction temperature on the vertical axis and a regression line is drawn, a straight line expressed as y = a _h x + b _h (0 < a _h ) is obtained. b _h on this line is T _SOR ' in the above-mentioned formula 6. When b _h is substituted for T _SOR ' in the above-mentioned formula 6 and the measured reaction temperature is substituted for T _t ^' , the deterioration degree Φ' after any reaction t days has elapsed can be obtained. When the reaction time is plotted on the horizontal axis and the logarithm of Φ' on the vertical axis and a regression line is drawn, a straight line expressed as y = - a _h ^' x (|- _{a h} ^' | = a _h ^' ) is obtained. a _h ^' represents the catalyst deterioration rate.

The same reaction is carried out for h types of hydrogen/feed oil ratios _Gh , h a _h and b _h are determined in the same manner, and h a _h ^' are obtained by the same method as above. h is an integer of 3 or more. The larger the number of h, the more accurate b can be obtained. On the other hand, if the number 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 's and G _h's thus obtained are respectively substituted into the following formula 11. The following formula 11 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.

ln( _ah ')=-bln( _Gh )+B3 Equation 11
In the formula 11, B3 can be 0.

For h combinations of a _h ' and G _h , ln(a _h ') is plotted on the vertical axis and ln(G _h ) on the horizontal axis, a regression line is drawn, and the slope is determined. This slope is the hydrogen/feed oil ratio coefficient b.

Moreover, _GB can be obtained by averaging the above h types of hydrogen/feedstock ratios _Gh .

In determining b and _GB , 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 an actual plant.
Such an LHSV is, for example, 0.5 to 2.5 h ⁻¹ , the hydrogen partial pressure is, for example, 3 to 7 MPa, the sulfur concentration in the feed oil is, for example, 0.5 to 3.0 mass%, and the sulfur concentration in the product oil is, for example, 0.3 mass% or less.
Similarly, it is preferable that the hydrogen/feedstock ratio G _h of the h types is set to a condition that corresponds to the actual operating conditions. Such G _h is, for example, 100 to 400 [Nm ³ /kL]. The reaction period is, for example, 50 to 600 days.

Moreover, α′ can be calculated by the same method as the method for calculating α described in the degradation function 1 ((method 1 for calculating α and T _SOR ) and (method 2 for calculating α and T _SOR )), except that the formula 10 is used instead of the formula 3.

<Deterioration function 2>
In this embodiment, the coke deterioration function relating to catalyst deterioration due to coke deposition is preferably deterioration function 2, expressed by the following equation 12, which is composed of an easily deactivated active species deterioration function relating to the deterioration of easily deactivated active species of the catalyst and a hardly deactivated active species deterioration function relating to the deterioration of hardly deactivated active species of the catalyst.

Φ=k ₁ ×exp(-D ₁ t)+k ₂ ×exp(-D ₂ t) Equation 12
In Equation 12, _k1 is the active site coefficient of the easily deactivated active species of the catalyst, _k2 is the active site coefficient of the hardly deactivated active species of the catalyst, and the active site coefficients represent the relative reaction rate constants of both active species. _D1 is the deterioration coefficient of the easily deactivated active species of the catalyst, _D2 is the deterioration coefficient of the hardly deactivated active species of the catalyst, t is the number of days elapsed since the reaction began, and _k1 + _k2 = 1.

As mentioned above, in the hydrotreating reaction of vacuum distillation gas oil, catalyst degradation occurs due to coke buildup, so operation must be carried out at an elevated reaction temperature to maintain the sulfur content of the resulting oil below a certain level. In the hydrotreating reaction of vacuum distillation gas oil, the reaction temperature rises rapidly at the beginning of the reaction. This rapid rise in reaction temperature indicates rapid catalyst degradation at the beginning of the reaction. On the other hand, from the middle of the reaction onwards, the reaction temperature rises gradually. This gradual rise in reaction temperature indicates gradual catalyst degradation at the middle of the reaction onwards.

In other words, the profile of reaction temperature versus reaction time suggests that in the hydrotreating reaction of vacuum distillation gas oil, rapid catalyst deterioration occurs at the beginning of the reaction, followed by gradual catalyst deterioration from the middle of the reaction onwards.

The inventors of the present application further improved Degradation Function 1 and discovered Degradation Function 2 based on the above-mentioned profile of reaction temperature versus reaction time and the assumption that catalysts contain active species that are easily deactivated in the early stages of the reaction and active species that are difficult to deactivate in the middle or later stages of the reaction. As a result, they found that Degradation Function 2 makes it possible to calculate the degree of catalyst degradation more accurately than Degradation Function 1. Easily deactivated active species are active species that lose activity mainly in the early stages of the reaction, and difficult to deactivate active species are active species that lose activity in the middle or later stages of the reaction.

In the formula 12, _k1 represents the active site coefficient of the easily deactivated active species of the catalyst, and _k2 represents the active site coefficient of the hardly deactivated active species of the catalyst. _k1 and _k2 are constants specific to the catalyst, and the method for determining them will be described later.

_D1 can be calculated by the following formula 13, and _D2 can be calculated by the following formula 14.

In the above formulas 13 and 14, S _F is the sulfur concentration (mass%) in the feedstock oil after t days of reaction, 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 vacuum distillation gas oil, LHSV is the liquid hourly space velocity (h ⁻¹ ) after t days of reaction, P _B is the reference hydrogen partial pressure (MPa), P is the hydrogen partial pressure (MPa) after t days of reaction, a is the hydrogen partial pressure coefficient, Ec is the activation energy of coke deterioration (kJ/mol), R is the gas constant: 0.00831 (kJ/(mol·K)), T _B is the reference reaction temperature (K), and T _SOR is the required temperature on day 0 (K).
In the above formula 13, _α1 is a catalytic constant (a constant representing the deterioration rate of the catalyst) of the easily deactivated active site, and in the above formula 14, _α2 is a catalytic constant (a constant representing the deterioration rate of the catalyst) of the hardly deactivated active site.

In the above-mentioned formulas 13 and 14, S _F , S _P , LHSV, and P 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 above-mentioned information acquisition step, as in the explanation of the above-mentioned formula 3. Note that the LHSV can be calculated by dividing the feed oil supply rate (volume/h) by the catalyst loading amount (volume).

As described above, S _F , LHSV, and P are controllable parameters. Furthermore, S _P is the sulfur concentration of the target product oil. That is, the deterioration coefficient of the catalyst's easily deactivated active species and the deterioration coefficient of the catalyst's less easily deactivated active species under the reaction conditions of S _F , S _P , LHSV, and P can be calculated using Equation 13 and Equation 14, respectively. The method for determining n, which is the reaction order of the hydrotreating reaction of feedstock oil containing vacuum distillation gas oil, will be described later.

(How to determine basic degradation parameters)
In the above-mentioned formulas 13 and 14, α ₁ , α ₂ , P _B , a, Ec, T _B , and T _SOR are constants, as in the above-mentioned formula 3, 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 performing a reaction in an actual machine, or may be determined in advance on a bench scale based on the actual machine operating conditions. In this embodiment, it is preferable to determine it in advance on a bench scale based on the actual machine operating conditions. In the above-mentioned formulas 13 and 14, P _B , a, Ec, and T _B can be determined by the same method as in the above-mentioned formula 3.
On the other hand, α ₁ , α ₂ and T _SOR can be calculated, for example, by the following two methods. In addition, the active site coefficient k ₁ of the easily deactivated active species of the catalyst and the active site coefficient k ₂ of the hardly deactivated active species of the catalyst in the above formula 12 can also be calculated simultaneously as follows.

(Method 1 for determining α ₁ , α _{2 ,} T _SOR , k ₁ , and k ₂ )
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, operation is carried out while increasing the reaction temperature. Reaction time is plotted on the horizontal axis and reaction temperature on the vertical axis. When drawing a regression line between these plots, as described above, two lines are obtained: one line expressed as y = a ₁ x + b ₁ , which correlates with the rapid increase in reaction temperature in the early stage of the reaction (x ₁ to x _n ), and the other line expressed as y = a ₂ x + b ₂ , which correlates with the gradual increase in reaction temperature from the middle stage of the reaction onwards (x n+ ₁ to x _m ). In the above formula, a ₁ > a ₂ > 0, b ₁ < b ₂ , and x ₁ < x _n < x _n+1 < x _m . x _n and x _m represent the reaction time relative to the n(m)th plot from the start of the reaction.

The above-mentioned _a1 is a value correlated with _α1 , _b1 is a value correlated with _k1 + _k2 , and is T _SOR . Furthermore, _a2 is a value correlated with _α2 , and _b2 is a value correlated with _k2 . Next, the intersection point (x _ip , y _ip ) at y = a ₁ x + b ₁ and y = a ₂ x + b ₂ is calculated. This intersection point means the inflection point of y = a ₁ x + b ₁ and y = a ₂ x + b _2. In other words, up to (x _ip , y _ip ), only active species of the catalyst that are easily deactivated are considered to exist, and from (x _ip , y _ip ), two active species are considered to exist: an active species of the catalyst that is easily deactivated and an active species that is difficult to deactivate.

In Equation 6, substituting _b1 for T _SOR ' and substituting the reaction temperature for T _t ' will give the degree of deterioration Φ' after any t days of reaction. Plotting the reaction time on the horizontal axis and the logarithm of Φ' on the vertical axis and drawing a regression line from x ₁ to x _ip will give a line expressed as y = -a ₁ ^' x (|-a ₁ ^' | = a ₁ ^' ). Furthermore, drawing a regression line from x _ip to x _m will give a line expressed as y = -a ₂ ^' x -b ₂ ^' (|-a ₂ ^' | = a ₂ ^' and |-b ₂ ^' | = b ₂ ^' ). _{a 1} ^' is a value correlated with α ₁ , a ₂ ^' is a value correlated with α ₂ , and b ₂ ^' is a value correlated with k ₂ .

_k2 can be found by substituting _b2 ^' obtained from the regression line described above into the following formula 15. Since _k1 is _k1 + _k2 = 1, k1 can be found from _k1 = 1 - _k2 .
k ₂ =exp(-b ₂ ^' ) Equation 15

D1 and D2 are obtained by substituting the operating conditions S _P , S _F , LHSV, and P, as well as P _B , a, Ec, T _B , and T _SOR (b ₁ ) obtained by the above method, into the above equations ₁₃ and _14. Φ is obtained by substituting the obtained D ₁ , D ₂ , k ₁ , and k ₂ into the above equation 12. In this case, Φ is a function of α ₁ and α ₂ . 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 from x ₁ to x _ip while setting α ₂ =0 and changing α ₁ so that 0 < α ₁ , multiple lines expressed as y = -a _α1 ^'' x (|-a _α1 ^'' | = a _α1 ^'' ) will be obtained for each value of α _1. The α 1 when a _α1 ^'' on each line is equal to the above-mentioned a ₁ ^' can be taken as _{the α 1 in} the above formula 13.
Next, by substituting the obtained α1 into Φ, which is a function of _α1 and _α2 obtained by the _above method, and drawing a regression line from x _ip to x _m while changing _α2 so that 0 < _α2 , multiple lines expressed as y = -a _α2 ^" x - b _α2 ^" (|-a _α2 ^" | = a _α2 ^" ) are obtained for each value of _α2 . The α2 when a _α2 ^" on each line is equal to the above-mentioned a ₂ ^' can be taken as the _α2 in the above formula 14 _.

(Method 2 for determining α ₁ , α _{2 ,} T _SOR , k ₁ , and k ₂ )
A reaction similar to that in (Method 1 for determining _α1 , α2 _, T _SOR , _k1 , and _k2 ) is carried out to obtain T _SOR ( _b1 ). D1 and D2 are obtained by substituting the operating conditions S _P , _SF , LHSV, and P, as well as P _B , a, Ec, T _B , and T _SOR ( _b1 ) determined by the above-described method, into Equations 13 and _14. Φ is obtained by substituting _the determined _D1 and _D2 into Equation 12. In this case, Φ is a function of _α1 , _α2 , _k1 , and _k2 . Substituting the obtained Φ for Φ' in the above formula 6 and T _SOR (i.e., b ₁ ) for T _SOR ^' in the above formula 6 and rearranging for T _t ^' , T _t ^' becomes a function of α ₁ , α ₂ , k ₁ , and k _2. If α ₂ is set to 0 and k ₂ = 1 - k ₁ , T _t ^' becomes a function of α ₁ and k _1. The combination of α 1 and k ₁ when the ratio of T _t ^' to the actually measured reaction temperature T _obs at x ₁ to x _ip (T _t ^' /T _obs ) is ₁ can be found, and this α ₁ can be used as α ₁ in the above formula 13. Note that k ₁ at this time is a provisional value. Similarly, it is preferable to calculate the ratio of T _t ^' to M reaction temperatures T _obs (T _t ^' /T _obs ), and define α ₁ when the average of these is closest to 1 as α ₁ in the above formula 13. M is an integer of 10 or more, preferably 10 to 500, and more preferably 50 to 200.
Using the obtained _α1 and setting _k1 = 1 - _k2 , _Tt ^' becomes a function of _α2 and _k2 . The combination of α2 and _k2 when the ratio ( _Tt ^' / _Tobs ) of Tt ^' to the actually measured reaction temperature _Tobs at _xip to _xm is 1 is found, and _{these α2} and _k2 can be used as _{α2 and k2} in the above formula 14. By substituting the obtained _k2 into _k1 = 1 - _k2 , _k1 is found, and this _k1 can be used as _k1 in the above formula 13. Similarly, it is preferable to calculate the ratios ( _Tt ^' / _Tobs ) of _Tt ^' to L reaction temperatures _Tobs , and use the _α2 and _k2 when the average of these is closest to 1 as the _α2 and _k2 in the above formula 14. It is also preferable that _k1 calculated from the obtained _k2 is used as _k1 in the above formula 13. L is an integer of 10 or more, preferably 10 to 500, and more preferably 50 to 200.

In this way, in order to find α ₁ , α _{2 ,} T _SOR , k ₁ , and k ₂ , it is necessary to obtain y = a ₁ x + b ₁ and y = a ₂ x + b _2. For example, y = a ₁ x + b ₁ and y = a ₂ x + b ₂ can be found as follows.

Using the method described above, the reaction time is plotted on the horizontal axis and the reaction temperature on the vertical axis. By drawing a regression line from the start of the reaction to the end of the reaction, a straight line expressed as y = a'x + b' is obtained. This line does not take into account the inflection point. Plots are sequentially deleted from the end of the reaction, and the y = a'x + b' is adjusted so that the correlation coefficient approaches 1, resulting in y = _a1'x + _b1 '. Similarly, plots are sequentially deleted from the start of the reaction, and the y = a'x + b' is adjusted so that the correlation coefficient approaches ₁ , resulting in 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 belong to either y=a ₁ x+b ₁ or y=a ₂ x+b ₂ .

The reaction time required to obtain y = a ₁ x + b ₁ and y = a ₂ x + b ₂ 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 more.

(Modification of degradation function 2)
The following describes a modification of the point spread function 2. Point spread function 2-1 expressed by the following equation 16 may be used as the point spread function 1.

Φ=k ₁ × exp (-D ₁ 't) + k ₂ × exp (-D ₂ 't) Equation 16
In the formula 16, k ₁ , k ₂ and t are the same as in the formula 12, D ₁ ' is the deactivation coefficient of the easily deactivated active species of the catalyst, and D ₂ ' is the deactivation coefficient of the hardly deactivated active species of the catalyst.

D ₁ ' can be calculated from the following formula 17, and D ₂ ' can be calculated from the following formula 18.

In the formulas 17 and 18, S _F , S _P , n, LHSV, P _B , P, a, Ec, R, T _B , and T _SOR are the same as in the formulas 13 and 14, G _B , G, and b are the same as in the formula 10, in the formula 17, α ₁ ' is a catalytic constant (a constant representing the deterioration rate of the catalyst) of the easily deactivated active site, and in the formula 18, α ₂ ' is a catalytic constant (a constant representing the deterioration rate of the catalyst) of the hardly deactivated active site.

P _B , a, Ec, T _B , and T _SOR can be calculated in the same manner as described in Equation 13 and Equation 14, and G _B and b can be calculated in the same manner as described in Equation 10.

In addition, α ₁ ' and α ₂ ' can be calculated in the same manner as for calculating α ₁ and α ₂ described in degradation function 2, except that equation 16 is used instead of equation 12, equation 17 is used instead of equation 13, and equation 18 is used instead of equation 14.

<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 feed oil, the information on the product oil, and the operating conditions based on the degree of catalyst deterioration. The reaction temperature is preferably calculated using a deterioration rate equation based on the Arrhenius equation.

<Deterioration rate formula>
The deterioration rate equation is based on the Arrhenius equation expressed by the above-mentioned equation 5. Similar to the calculation method of the above-mentioned equation 6, the following equation 19 is derived from the above-mentioned equations 1 and 5.

In Equation 19, Φ is the degree of deterioration, Ea is the activation energy of desulfurization (kJ/mol), R is the gas constant: 0.00831 (kJ/(mol·K)), _Tt is the required temperature (K) after t days of reaction, and T _SOR is the required temperature (K) on day 0.
By rearranging the above equation 19, the following equation 20 is obtained.

T _t (K) after t days of reaction can be obtained by substituting T _SOR and Φ obtained by the above-mentioned method into the above-mentioned formula 20. The activation energy of the desulfurization reaction in the above-mentioned formula 20 can be calculated as follows.

(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 5. An example will be described below.

First, the reaction order of the desulfurization reaction of feedstock oil containing vacuum distillation gas oil is determined. The reaction temperature, hydrogen partial pressure, hydrogen/feedstock ratio, and sulfur concentration in the feedstock oil are constant, and the reaction is carried out under LHSV(x) conditions, and the sulfur concentration in the product oil is measured. In the desulfurization reaction rate equation expressed by the following equation 21, the sulfur concentration in the feedstock oil is substituted for _SF , the sulfur concentration in the resulting product oil for _SP , and LHSV(x) for LHSV. The result of the left-hand side of the equation is plotted on the vertical axis and 1/LHSV on the horizontal axis. In this case, the vertical axis is a function of n.

A similar reaction is carried out for x types of LHSV(x), and x of the above plots are obtained. Based on the obtained plots, a regression line is drawn passing 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 ))), x is 1/LHSV, and c is k. The correlation function is calculated using Excel or similar software, and n is determined for which the correlation coefficient is closest to 1. The obtained n is the reaction order. Note that n can be calculated to one decimal place.

The above x is an integer of 3 or greater. 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 inefficient. In this embodiment, x is preferably 3 to 20, and more preferably 3 to 10.

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.
Such a reaction temperature is, for example, 300 to 420°C, the hydrogen partial pressure is 3 to 7 MPa, the hydrogen/feedstock ratio is 100 to 400 [Nm ³ /kL], and the sulfur concentration in the feedstock is 0.5 to 3.0 mass%.
Similarly, it is preferable that the x types of LHSV(x) are set to conditions that correspond to the actual operating conditions of the plant. Such LHSV(x) is 0.5 to 2.5 h ⁻¹ .

When the activation energy E in the Arrhenius equation expressed by the above formula 5 is set as the activation energy Ea of desulfurization and the natural logarithm of both sides is taken, the following formula 22 is obtained.

The reaction is carried out under constant conditions of hydrogen partial pressure, hydrogen/feed oil ratio, LHSV, and sulfur concentration in the feed oil at a reaction temperature T(y), and the sulfur concentration in the product oil is measured. The sulfur concentration in the feed oil is substituted for _SF , the sulfur concentration in the resulting product oil for _SP , LHSV for LHSV, and the obtained n in the desulfurization reaction rate equation expressed by Equation 21 above are substituted for LHSV, and the reaction rate constant k is calculated. The obtained reaction rate constant is substituted into Equation 22 above, and the result (lnk) on the left side of the equation obtained is plotted on the vertical axis and 1/T (1/T(y)) on the horizontal axis.

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

The above y is an integer of 3 or greater. The larger the value of y, the more accurate Ea can be obtained. On the other hand, if the value of y is too large, it takes a long time to obtain Ea, which is inefficient. In this embodiment, y is preferably 3 to 20, and more preferably 3 to 10.

The hydrogen partial pressure, hydrogen/feed oil ratio, LHSV, and sulfur concentration in the feed oil used to determine Ea are preferably set to conditions that correspond to the operating conditions of an actual plant.
Such hydrogen partial pressure is, for example, 3 to 7 MPa, the hydrogen/feedstock ratio is 100 to 400 [Nm ³ /kL], the LHSV is 0.5 to 2.5 h ⁻¹ , and the sulfur concentration in the feedstock is 0.5 to 3.0 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 420°C.

By substituting each parameter thus obtained into the above-mentioned formula 20, the reaction temperature _Tt required to achieve the predetermined reaction conditions can be obtained.

The ratio of the reaction temperature _Tt determined by the information processing method of this embodiment to the actually measured reaction temperature _Tobs , _Tt / _Tobs , is preferably 0.97 to 1.03, and more preferably 0.985 to 1.015, in ° C. When _Tt / _Tobs is within the above range, it can be determined that the reaction temperature has been estimated with high accuracy.

<Information output step>
The method may further include an information output step (S4 in FIG. 1) of outputting information indicating the reaction temperature thus obtained. For example, S4 is executed by the output unit 14.

<Hydrotreatment reaction of feedstock oil containing vacuum distillation gas oil>
The hydrotreating reaction of feedstock oil containing vacuum distillation gas oil will be outlined below.
Vacuum distillation gas oil is a fraction having a boiling point range of 200 to 550°C obtained by vacuum distillation of atmospheric distillation residual oil. The density of vacuum distillation gas oil is 0.91 to 0.95 g/mL. The content of vacuum distillation gas oil in the feedstock oil may be, for example, 30% by volume or more, or 50% by volume or more.
In addition, examples of oil types other than vacuum distillation light oil contained in the feedstock include atmospheric heavy oil obtained by atmospheric distillation of crude oil in an atmospheric distillation unit, heavy extracts which are particularly heavy oils among the oils extracted and removed by solvent extraction of lubricating base oils such as hydrocracked heavy oil, atmospheric distillation residue, fluid catalytic cracking residue, and de-sludge oil.

The hydrotreating reaction of a feedstock containing vacuum gas oil can be carried out by contacting the feedstock containing vacuum gas oil with a hydrotreating catalyst in the presence of hydrogen.
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 among aluminas, γ-alumina being particularly preferred. These inorganic oxides may be used alone or in combination of two or more.

The metal contained in the support as an active component is at least one metal selected from Group 6 and Groups 8-10 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 10-25 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 low, preventing hydrotreating activity (hereinafter simply referred to as hydrotreating activity), including desulfurization activity. Conversely, if the supported metal content is greater than 25 mass%, metal aggregation occurs, reducing the number of active sites and, as a result, reducing hydrotreating activity. Furthermore, if necessary, phosphorus, boron, zinc, zirconia, etc. can be contained in addition to the active metals consisting of Groups 6 and 8 of the Periodic Table. When applying the method of the present invention, there are no restrictions on the form of the catalyst bed, and it can be applied to catalyst bed reactors such as fixed beds, moving beds, and fluidized beds.

The conditions for the hydrotreating reaction of feedstock containing vacuum distillation gas oil are generally a reaction temperature of 300 to 420°C, preferably 340 to 400°C, a hydrogen partial pressure of 3 to 7 MPa, preferably 4 to 6 MPa, an LHSV of 0.5 to 2.5 hr ^-1 , preferably 0.6 to 1.5 hr ^-1 , and a hydrogen/feedstock ratio of 100 to 400 [Nm ³ /kL], preferably 200 to 300 [Nm ³ /kL].

The sulfur concentration in feedstock oil, including vacuum distillation diesel, is typically 0.5 to 3.0 mass%. The sulfur concentration in the resulting oil is typically 0.01 to 0.3 mass%.

<Reaction temperature calculation device>
The reaction temperature calculation device of this embodiment is for a hydrotreating reaction of a feedstock containing vacuum distillation gas oil obtained by vacuum distillation of atmospheric distillation residue oil. The reaction temperature calculation device acquires information about the feedstock, information about the product oil, and information about the operating conditions after a predetermined time has elapsed since the start of the reaction, and calculates the catalyst degradation level using a degradation function based on the information about the feedstock, information about the product oil, and information about the operating conditions acquired by the acquisition unit. The reaction temperature calculation device of this embodiment may have an output unit that outputs information indicating the calculated reaction temperature.

The reaction temperature calculation device 1 of this embodiment is configured using an information processing device such as a personal computer, a server device, or a dedicated device. The reaction temperature calculation device 1 may be configured using one or more information processing devices. For example, the reaction temperature calculation device 1 may be configured as a cluster machine, a cloud, or any other configuration. The reaction temperature calculation device 1 includes, for example, an acquisition unit 11 and a computer main unit 12 that processes information from the acquisition unit, as shown in FIG. 4 . The reaction temperature calculation device 1 may also include an output unit 14 that outputs information processed by the computer main unit 12 to the outside. These components are implemented 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 implemented by hardware (including circuitry) such as an LSI (Large Scale Integrated Circuit), ASIC (Application Specific Integrated Circuit), FPGA (Field-Programmable Gate Array), or GPU (Graphics Processing Unit), or by a combination of software and hardware. The program may be stored in advance in a storage device (a storage device with a non-transitory storage medium) such as a hard disk drive (HDD) or flash memory, or it 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 composed of, for example, a HDD, flash memory, EEPROM (Electrically Erasable Programmable Read Only Memory), ROM (Read Only Memory), or RAM (Random Access Memory).

The acquisition unit 11 receives predetermined information input by the reaction operator and transmits the information acquired through this input to the computer main body 12. The information acquired by the acquisition unit 11 in this embodiment is, for the hydrotreating reaction of feedstock oil containing vacuum distillation gas oil, information on the feedstock oil a predetermined time after the start of the reaction, information on the product oil, and information on the operating conditions. The information on the feedstock oil a predetermined time after the start of the reaction, information on the product oil, and information on the operating conditions 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 on the feedstock oil a predetermined time after the start of the reaction, information on the product oil, and information on the operating conditions, and there are no particular limitations on the acquisition method.

In this embodiment, the acquisition unit 11 is configured with a single keyboard. The specific configuration of the acquisition unit 11 is not limited, and although it is a keyboard in this embodiment, it may also be a touch panel or the like. It is also possible for acquisition units that acquire various types of information to be configured separately and each to be independently connected to the computer main body 12. The acquisition unit 11 may also be configured to directly acquire each of the above-mentioned information via wired or wireless connections from a computer or the like used for controlling the reactor, etc.

The computer main body 12 is, for example, a so-called computer capable of processing various types of information. The computer main body 12 is equipped with an arithmetic unit 13. For example, a predetermined program is installed in the computer main body 12, and the arithmetic unit 13 is functionally configured by executing this program. Specifically, the arithmetic unit 13 calculates the degree of catalyst deterioration using a deterioration function based on information about the feedstock oil, information about the product oil, and information about the operating conditions acquired by the acquisition unit 11 a predetermined time after the start of the reaction, and calculates the reaction temperature required to satisfy the information about the feedstock oil, information about the product oil, and the operating conditions based on the degree of catalyst deterioration. The deterioration function is as described above. As described above, the reaction temperature can be determined, for example, from a deterioration rate equation. For example, the arithmetic unit 13 executes the deterioration degree calculation step and reaction temperature calculation step described above. The calculation unit 13 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 may be a microcontroller such as an MCU.

The calculation unit 13 may output to the output unit 14 information regarding the feedstock oil obtained as described above, information regarding the product oil, and information indicating the reaction temperature required to satisfy the operating conditions.

The output unit 14 receives the calculation results (reaction temperatures) output by the computer main body 12 (more specifically, the calculation unit 13) and outputs the received calculation results to the outside. In this embodiment, the output unit 14 is configured as a display unit such as a CRT display, LCD display, or PDP, but is not limited to this 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 feedstock oil including vacuum distillation diesel). The output unit 14 may also be a combination of these. For example, the output unit 14 executes the information output step described above.

In addition, this embodiment provides a reaction temperature calculation program for causing a computer to function as a reaction temperature calculation device, and a non-transitory computer-readable recording medium storing the program. Examples of non-transitory computer-readable recording media include magnetic tape (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 memory (such as solid-state drives (SSDs), memory cards, and USB memory).

<Method of using the information processing method and reaction temperature calculation device>
The information processing method and reaction temperature calculation device of this embodiment can estimate the reaction temperature required to achieve specified reaction conditions for the hydrotreating reaction of feedstock oil containing vacuum distillation gas oil. The information processing method and reaction temperature calculation device of this embodiment can obtain a plot of estimated reaction temperatures over time. The relationship between the plot and the maximum equipment operating temperature, etc., can be used in the following ways:

A first application method is to estimate the operating time (number of days) required to replace a catalyst under specified reaction conditions. That is, the plot can be used to estimate the time required to reach the maximum equipment operating temperature, and from that time, the operating time (number of days) required to replace the catalyst can be estimated. Furthermore, if the estimated reaction temperature is not equal to or lower than the equipment set temperature, an information processing method shown in S4-1 to S4-3 of FIG. 2 may be performed. The information processing method shown in S4-1 to S4-3 of FIG. 2 includes an information acquisition step (S4-1 of FIG. 2) for acquiring information about the target reaction temperature; a deterioration degree calculation step (S4-2 of FIG. 2) for calculating the catalyst deterioration level using a deterioration function based on the acquired target reaction temperature; and a reaction condition calculation step (S4-3 of FIG. 2) for calculating information about the feedstock oil, information about the product oil, and information about the operating conditions required to achieve the target reaction temperature based on the deterioration degree. The method may further include an information output step (S4-4 of FIG. 2) for outputting the information about the feedstock oil, information about the product oil, and information about the operating conditions obtained in this manner. Specifically, for example, when using degradation function 1, the target reaction temperature is substituted for _Tt in equation 19 to obtain Φ. The obtained Φ is substituted into equation 2 to obtain D. The obtained D is substituted into equation 3 to obtain a combination of S _P , S _F , LHSV, and P such that the equality of equation 3 is established. Furthermore, in the above combination, for example, S _P and S _F may be set as set values to obtain P and LHSV. Furthermore, any of degradation function 1, degradation function 1-1, degradation function 2, and degradation function 2-1 may be used as the degradation function. Note that each of the above steps is executed, for example, by the reaction temperature calculation device 1 of this embodiment. For example, S4-1 is executed by the acquisition unit 11, S4-2 and S4-3 are executed by the calculation unit 13 in the computer main body 12, and S4-4 is executed by the output unit 14. Note that the target temperature may be stored in advance in the calculation unit 13 in the computer main body 12.

A second utilization method is to estimate reaction conditions (throughput (LHSV), etc.) for achieving a predetermined operating time. Such an information processing method is represented by S1A to S3A in FIG. 3. The information processing method represented by S1A to S3A in FIG. 3 includes an information acquisition step (S1A in FIG. 3) for acquiring information about a target reaction temperature at a predetermined operating time; a deterioration degree calculation step (S2A in FIG. 3) for calculating a catalyst deterioration level using a deterioration function based on the acquired target reaction temperature; and a reaction condition calculation step (S3A in FIG. 3) for calculating information about the feed oil, information about the product oil, and information about the operating conditions necessary to achieve the target reaction temperature based on the deterioration level. The method may further include an information output step (S4A in FIG. 3) for outputting the information about the feed oil, information about the product oil, and information about the operating conditions obtained in this manner. Specifically, for example, when deterioration function 1 is used, the target reaction temperature after a predetermined operating time of t days has elapsed is substituted for T _t in Equation 19 to obtain Φ. The obtained Φ is substituted into Equation 2 to obtain D. The obtained D can be substituted into Equation 3 to find a combination of S _P , S _F , LHSV, and P that satisfies the equation of Equation 3. In the above combinations, for example, S _P and S _F may be set as set values to find P and LHSV. As the degradation function, any of degradation function 1, degradation function 1-1, degradation function 2, and degradation function 2-1 may be used. Note that each of the above steps is executed, for example, by the reaction temperature calculation device 1 of this embodiment. For example, S1A is executed by the acquisition unit 11, S2A and S3A are executed by the calculation unit 13 in the computer main body 12, and S4A is executed by the output unit 14. Note that the target temperature for a predetermined operation time may be stored in advance in the calculation unit 13 in the computer main body 12.

The present invention will be explained in more detail below using examples, but the present invention is not limited to the following examples.

[Example]
A bench-scale hydrotreating reaction was carried out by contacting a feedstock containing 70% by volume of vacuum distillation gas oil with a hydrotreating catalyst. Based on the results obtained, a degradation function was calculated. In this example, degradation function 2, expressed by Equation 12, was used. The parameters in Equations 12 to 14 were calculated using the method described above, resulting in k ₁ =0.9, k ₂ =0.1, α ₁ =0.001, α ₂ =0.0005, P _B =4.9 (MPa), a =0.6, Ec =150 (kJ/mol), T _B =673 (K), T _SOR =630 (K), and n =1.5.

The reaction was carried out in an actual plant using the same feedstock and hydrotreating catalyst as in the bench-scale hydrotreating reaction. The operating conditions in Equations 13 and 14 were S _F =2.62 (mass%), P =6.0 (MPa), LHSV =0.485 (h ⁻¹ ), and S _P =0.07 (mass%).
Furthermore, the activation energy of desulfurization was previously determined by the above-mentioned method and was found to be Ea = 125 (kJ/mol).
These basic degradation parameters and reaction conditions were substituted into the above formulas 13 and 14 to obtain _D1 and _D2 after any t days of reaction had elapsed. The obtained _D1 and _D2 and the number of days elapsed since reaction, t, were substituted into the above formula 12 to obtain Φ. The obtained Φ, Ea, and T _SOR were substituted into the above formula 20 to obtain the required temperature, _Tt, after any t days of reaction had elapsed. Table 1 shows the measured values of the reaction temperature at t = 251 days, 514 days, and 1164 days, the required temperature, _Tt , obtained by the above method, and the ratio of the required temperature, _Tt , to the measured value of the reaction temperature.

As shown in Table 1, it was found that the required temperature _Tt obtained by the present invention was almost equal to the actually measured value of the reaction temperature.

1... reaction temperature calculation device 11... acquisition unit 12... computer main body 13... calculation unit 14... output unit

Claims (10)

With respect to the hydrotreating reaction of feedstock oil including vacuum distillation gas oil obtained by vacuum distillation of atmospheric distillation residue oil, an information acquisition step of acquiring information on the feedstock oil, information on the product oil, and information on operating conditions at a predetermined time after the start of the reaction;
a deterioration degree calculation step of calculating a deterioration degree of the catalyst using a deterioration function based on the acquired information on the feed oil, the information on the product oil, and the information on the operating conditions;
and a reaction temperature calculation step of calculating information about the feed oil, information about the product oil, and a reaction temperature necessary to satisfy the operating conditions based on the deterioration degree of the catalyst ,
the information on the feed oil is information on a sulfur concentration in the feed oil, the information on the product oil is information on a sulfur concentration in the product oil, and the information on the operating conditions is information on a hydrogen partial pressure, information on a catalyst loading amount, and information on a feed amount of the feed oil;
The information processing method, wherein the degradation function is a function expressed by the following equation 2:
Φ=exp(-Dt) Formula 2
In the above formula 2, Φ is the degree of deterioration of the catalyst, D is the deterioration coefficient of the active species of the catalyst and is calculated using the following formula 3, and t is the number of days elapsed since the reaction began.
In the above formula 3, α is a catalyst constant (constant representing the catalyst deterioration rate), S _F is the sulfur concentration in the feed oil after t days of reaction (mass%), S _P is the sulfur concentration in the product oil after t days of reaction (mass%), n is the reaction order of the hydrotreating reaction of the feed oil containing vacuum distillation gas oil, LHSV is the liquid hourly space velocity (h -1 ⁾ after t days of reaction , P _B is the reference hydrogen partial pressure (MPa), P is the hydrogen partial pressure (MPa) after t days of reaction, a is the hydrogen partial pressure coefficient, Ec is the activation energy of coke deterioration (kJ / mol), R is the gas constant: 0.00831 (kJ / (mol · K)), T _B is the reference reaction temperature (K), and T _SOR is the required temperature on day 0 (K). α, P _B , a, Ec, T _B , and T _SOR are constants determined according to the catalyst used. The constants are determined while carrying out a reaction in an actual machine, or are determined in advance on a bench scale based on the operating conditions of the actual machine . With respect to the hydrotreating reaction of feedstock oil including vacuum distillation gas oil obtained by vacuum distillation of atmospheric distillation residue oil, an information acquisition step of acquiring information on the feedstock oil, information on the product oil, and information on operating conditions at a predetermined time after the start of the reaction;
a deterioration degree calculation step of calculating a deterioration degree of the catalyst using a deterioration function based on the acquired information on the feed oil, the information on the product oil, and the information on the operating conditions;
and a reaction temperature calculation step of calculating information about the feed oil, information about the product oil, and a reaction temperature necessary to satisfy the operating conditions based on the deterioration degree of the catalyst,
the information on the feed oil is information on the sulfur concentration in the feed oil, the information on the product oil is information on the sulfur concentration in the product oil, and the information on the operating conditions is information on the hydrogen partial pressure, information on the catalyst loading amount, information on the feed rate of the feed oil, and information on the hydrogen supply rate;
The information processing method, wherein the degradation function is a function expressed by the following equation 9:
Φ=exp(-D’t) Equation 9
In the above formula 9, Φ is the degree of deterioration of the catalyst, D′ is the deterioration coefficient of the active species of the catalyst and is calculated using the following formula 10, and t is the number of days elapsed since the reaction began.
In the above formula 10, α' is a catalyst constant (a constant representing the deterioration rate of the catalyst), and 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 vacuum distillation gas oil, 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 t days of reaction, a is the hydrogen partial pressure coefficient, and G _B is the standard hydrogen/feed oil ratio (Nm ³ /kL), G is the hydrogen/feedstock ratio (Nm ³ /kL), b is the hydrogen/feed oil ratio coefficient, Ec is the activation energy of coke deterioration (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. _B , a, G _B ,b,Ec,T _B , T _SOR is a constant determined depending on the catalyst used. The constant is determined while carrying out a reaction in an actual reactor, or is determined in advance on a bench scale based on the operating conditions of the actual reactor. With respect to the hydrotreating reaction of feedstock oil including vacuum distillation gas oil obtained by vacuum distillation of atmospheric distillation residue oil, an information acquisition step of acquiring information on the feedstock oil, information on the product oil, and information on operating conditions at a predetermined time after the start of the reaction;
a deterioration degree calculation step of calculating a deterioration degree of the catalyst using a deterioration function based on the acquired information on the feed oil, the information on the product oil, and the information on the operating conditions;
and a reaction temperature calculation step of calculating information about the feed oil, information about the product oil, and a reaction temperature necessary to satisfy the operating conditions based on the deterioration degree of the catalyst,
the information on the feed oil is information on a sulfur concentration in the feed oil, the information on the product oil is information on a sulfur concentration in the product oil, and the information on the operating conditions is information on a hydrogen partial pressure, information on a catalyst loading amount, and information on a feed amount of the feed oil;
The information processing method, wherein the degradation function is a function expressed by the following equation 12:
Φ=k ₁ ×exp(-D ₁ t) + k ₂ ×exp(-D ₂ t) Equation 12
In the formula 12, k ₁ is the active site coefficient of the easily deactivated active species of the catalyst, and k ₂ is the active site coefficient of the catalyst's resistant to deactivation, and the active site coefficient represents the relative reaction rate constant of both active species. ₁ is the deterioration coefficient of the easily deactivated active species of the catalyst, calculated from the following formula 13, and D ₂ is the deterioration coefficient of the catalyst's resistant to deactivation and is calculated using the following formula 14, t is the number of days elapsed since the reaction began (days), and k ₁ +k ₂ = 1, and k ₁ and k ₂ is determined while carrying out the reaction in an actual reactor, or is determined in advance on a bench scale based on the operating conditions of the actual reactor.
In the formula 13 and the formula 14, 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 vacuum distillation gas oil, 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 t days of reaction, a is the hydrogen partial pressure coefficient, Ec is the activation energy of coke deterioration (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 13, α ₁ is the catalytic constant of the easily deactivated active site (a constant representing the rate of catalyst deterioration), and in the above formula 14, α ₂ is the catalytic constant of the refractory active site (a constant that represents the rate of catalyst deterioration). ₁ , α ₂ , P _B , a, Ec, T _B , T _SOR is a constant determined depending on the catalyst used. The above constant is determined while carrying out the reaction in an actual reactor, or is determined in advance on a bench scale based on the operating conditions of the actual reactor. With respect to the hydrotreating reaction of feedstock oil including vacuum distillation gas oil obtained by vacuum distillation of atmospheric distillation residue oil, an information acquisition step of acquiring information on the feedstock oil, information on the product oil, and information on operating conditions at a predetermined time after the start of the reaction;
a deterioration degree calculation step of calculating a deterioration degree of the catalyst using a deterioration function based on the acquired information on the feed oil, the information on the product oil, and the information on the operating conditions;
and a reaction temperature calculation step of calculating information about the feed oil, information about the product oil, and a reaction temperature necessary to satisfy the operating conditions based on the deterioration degree of the catalyst,
the information on the feed oil is information on the sulfur concentration in the feed oil, the information on the product oil is information on the sulfur concentration in the product oil, and the information on the operating conditions is information on the hydrogen partial pressure, information on the catalyst loading amount, information on the feed rate of the feed oil, and information on the hydrogen supply rate;
The information processing method, wherein the degradation function is a function expressed by the following equation 16:
Φ=k ₁ ×exp(-D ₁ 't) + k ₂ ×exp(-D ₂ 't) Equation 16
In the formula 16, k ₁ is the active site coefficient of the easily deactivated active species of the catalyst, and k ₂ is the active site coefficient of the catalyst's resistant to deactivation, and the active site coefficient represents the relative reaction rate constant of both active species. ₁ ' is the deterioration coefficient of the easily deactivated active species of the catalyst, calculated by the following formula 17, D ₂ ' is the deterioration coefficient of the catalyst's resistant to deactivation active species, calculated using the following formula 18, t is the number of days elapsed since the reaction (days), and k ₁ +k ₂ = 1, and k ₁ and k ₂ is determined while carrying out the reaction in an actual reactor, or is determined in advance on a bench scale based on the operating conditions of the actual reactor.
In the formula 17 and the formula 18, 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 vacuum distillation gas oil, 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 t days of reaction, a is the hydrogen partial pressure coefficient, and G _B is the standard hydrogen/feed oil ratio (Nm ³ /kL), G is the hydrogen/feedstock ratio (Nm ³ /kL), b is the hydrogen/feed oil ratio coefficient, Ec is the activation energy of coke deterioration (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 17, α ₁ ' is a catalytic constant of the easily deactivated active site (a constant representing the deterioration rate of the catalyst), and in the above formula 18, α ₂ ' is the catalytic constant of the refractory active site (a constant that represents the rate of catalyst deterioration). ₁ ', α ₂ ', P _B , a, G _B ,b,Ec,T _B , T _SOR is a constant determined depending on the catalyst used. The above constant is determined while carrying out the reaction in an actual reactor, or is determined in advance on a bench scale based on the operating conditions of the actual reactor. An acquisition unit that acquires information about the feedstock oil, information about the product oil, and information about operating conditions at a predetermined time after the start of the reaction, regarding the hydrotreating reaction of the feedstock oil including the vacuum distillation gas oil obtained by vacuum distillation of the atmospheric distillation residue oil;
a calculation unit that calculates a catalyst degradation level using a degradation function based on the information about the feed oil, the information about the product oil, and the information about the operating conditions acquired by the acquisition unit, and calculates a reaction temperature necessary to satisfy the information about the feed oil, the information about the product oil, and the operating conditions based on the calculated catalyst degradation level,
the information on the feed oil is information on a sulfur concentration in the feed oil, the information on the product oil is information on a sulfur concentration in the product oil, and the information on the operating conditions is information on a hydrogen partial pressure, information on a catalyst loading amount, and information on a feed amount of the feed oil;
The reaction temperature calculation device, wherein the degradation function is a function expressed by the following equation 2:
Φ=exp(-Dt) Formula 2
In the above formula 2, Φ is the degree of deterioration of the catalyst, D is the deterioration coefficient of the active species of the catalyst and is calculated using the following formula 3, and t is the number of days elapsed since the reaction began.
In the above formula 3, α is a catalyst constant (constant representing the catalyst deterioration rate), S _F is the sulfur concentration in the feed oil after t days of reaction (mass%), S _P is the sulfur concentration in the product oil after t days of reaction (mass%), n is the reaction order of the hydrotreating reaction of the feed oil containing vacuum distillation gas oil, LHSV is the liquid hourly space velocity (h -1 ⁾ after t days of reaction , P _B is the reference hydrogen partial pressure (MPa), P is the hydrogen partial pressure (MPa) after t days of reaction, a is the hydrogen partial pressure coefficient, Ec is the activation energy of coke deterioration (kJ / mol), R is the gas constant: 0.00831 (kJ / (mol · K)), T _B is the reference reaction temperature (K), and T _SOR is the required temperature on day 0 (K). α, P _B , a, Ec, T _B , and T _SOR are constants determined according to the catalyst used. The constants are determined while carrying out a reaction in an actual machine, or are determined in advance on a bench scale based on the operating conditions of the actual machine . An acquisition unit that acquires information about the feedstock oil, information about the product oil, and information about operating conditions at a predetermined time after the start of the reaction, regarding the hydrotreating reaction of the feedstock oil including the vacuum distillation gas oil obtained by vacuum distillation of the atmospheric distillation residue oil;
a calculation unit that calculates a catalyst degradation level using a degradation function based on the information about the feed oil, the information about the product oil, and the information about the operating conditions acquired by the acquisition unit, and calculates a reaction temperature necessary to satisfy the information about the feed oil, the information about the product oil, and the operating conditions based on the calculated catalyst degradation level,
the information on the feed oil is information on the sulfur concentration in the feed oil, the information on the product oil is information on the sulfur concentration in the product oil, and the information on the operating conditions is information on the hydrogen partial pressure, information on the catalyst loading amount, information on the feed rate of the feed oil, and information on the hydrogen supply rate;
The reaction temperature calculation device, wherein the degradation function is a function expressed by the following equation 9.
Φ=exp(-D’t) Equation 9
In the above formula 9, Φ is the degree of deterioration of the catalyst, D′ is the deterioration coefficient of the active species of the catalyst and is calculated using the following formula 10, and t is the number of days elapsed since the reaction began.
In the above formula 10, α' is a catalyst constant (a constant representing the deterioration rate of the catalyst), and 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 vacuum distillation gas oil, 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 t days of reaction, a is the hydrogen partial pressure coefficient, and G _B is the standard hydrogen/feed oil ratio (Nm ³ /kL), G is the hydrogen/feedstock ratio (Nm ³ /kL), b is the hydrogen/feed oil ratio coefficient, Ec is the activation energy of coke deterioration (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. _B , a, G _B ,b,Ec,T _B , T _SOR is a constant determined depending on the catalyst used. The constant is determined while carrying out a reaction in an actual reactor, or is determined in advance on a bench scale based on the operating conditions of the actual reactor. An acquisition unit that acquires information about the feedstock oil, information about the product oil, and information about operating conditions at a predetermined time after the start of the reaction, regarding the hydrotreating reaction of the feedstock oil including the vacuum distillation gas oil obtained by vacuum distillation of the atmospheric distillation residue oil;
a calculation unit that calculates a catalyst degradation level using a degradation function based on the information about the feed oil, the information about the product oil, and the information about the operating conditions acquired by the acquisition unit, and calculates a reaction temperature necessary to satisfy the information about the feed oil, the information about the product oil, and the operating conditions based on the calculated catalyst degradation level,
the information on the feed oil is information on a sulfur concentration in the feed oil, the information on the product oil is information on a sulfur concentration in the product oil, and the information on the operating conditions is information on a hydrogen partial pressure, information on a catalyst loading amount, and information on a feed amount of the feed oil;
The reaction temperature calculation device, wherein the degradation function is a function expressed by the following equation 12:
Φ=k ₁ ×exp(-D ₁ t) + k ₂ ×exp(-D ₂ t) Equation 12
In the formula 12, k ₁ is the active site coefficient of the easily deactivated active species of the catalyst, and k ₂ is the active site coefficient of the catalyst's resistant to deactivation, and the active site coefficient represents the relative reaction rate constant of both active species. ₁ is the deterioration coefficient of the easily deactivated active species of the catalyst, calculated from the following formula 13, and D ₂ is the deterioration coefficient of the catalyst's resistant to deactivation and is calculated using the following formula 14, t is the number of days elapsed since the reaction began (days), and k ₁ +k ₂ = 1, and k ₁ and k ₂ is determined while carrying out the reaction in an actual reactor, or is determined in advance on a bench scale based on the operating conditions of the actual reactor.
In the formula 13 and the formula 14, 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 vacuum distillation gas oil, 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 t days of reaction, a is the hydrogen partial pressure coefficient, Ec is the activation energy of coke deterioration (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 13, α ₁ is the catalytic constant of the easily deactivated active site (a constant representing the rate of catalyst deterioration), and in the above formula 14, α ₂ is the catalytic constant of the refractory active site (a constant that represents the rate of catalyst deterioration). ₁ , α ₂ , P _B , a, Ec, T _B , T _SOR is a constant determined depending on the catalyst used. The above constant is determined while carrying out the reaction in an actual reactor, or is determined in advance on a bench scale based on the operating conditions of the actual reactor. An acquisition unit that acquires information about the feedstock oil, information about the product oil, and information about operating conditions at a predetermined time after the start of the reaction, regarding the hydrotreating reaction of the feedstock oil including the vacuum distillation gas oil obtained by vacuum distillation of the atmospheric distillation residue oil;
a calculation unit that calculates a catalyst degradation level using a degradation function based on the information about the feed oil, the information about the product oil, and the information about the operating conditions acquired by the acquisition unit, and calculates a reaction temperature necessary to satisfy the information about the feed oil, the information about the product oil, and the operating conditions based on the calculated catalyst degradation level,
the information on the feed oil is information on the sulfur concentration in the feed oil, the information on the product oil is information on the sulfur concentration in the product oil, and the information on the operating conditions is information on the hydrogen partial pressure, information on the catalyst loading amount, information on the feed rate of the feed oil, and information on the hydrogen supply rate;
The reaction temperature calculation device, wherein the degradation function is a function expressed by the following equation 16.
Φ=k ₁ ×exp(-D ₁ 't) + k ₂ ×exp(-D ₂ 't) Equation 16
In the formula 16, k ₁ is the active site coefficient of the easily deactivated active species of the catalyst, and k ₂ is the active site coefficient of the catalyst's resistant to deactivation, and the active site coefficient represents the relative reaction rate constant of both active species. ₁ ' is the deterioration coefficient of the easily deactivated active species of the catalyst, calculated by the following formula 17, D ₂ ' is the deterioration coefficient of the catalyst's resistant to deactivation active species, calculated using the following formula 18, t is the number of days elapsed since the reaction (days), and k ₁ +k ₂ = 1, and k ₁ and k ₂ is determined while carrying out the reaction in an actual reactor, or is determined in advance on a bench scale based on the operating conditions of the actual reactor.
In the formula 17 and the formula 18, 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 vacuum distillation gas oil, 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 t days of reaction, a is the hydrogen partial pressure coefficient, and G _B is the standard hydrogen/feed oil ratio (Nm ³ /kL), G is the hydrogen/feedstock ratio (Nm ³ /kL), b is the hydrogen/feed oil ratio coefficient, Ec is the activation energy of coke deterioration (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 17, α ₁ ' is a catalytic constant of the easily deactivated active site (a constant representing the deterioration rate of the catalyst), and in the above formula 18, α ₂ ' is the catalytic constant of the refractory active site (a constant that represents the rate of catalyst deterioration). ₁ ', α ₂ ', P _B , a, G _B ,b,Ec,T _B , T _SOR is a constant determined depending on the catalyst used. The above constant is determined while carrying out the reaction in an actual reactor, or is determined in advance on a bench scale based on the operating conditions of the actual reactor. A reaction temperature calculation program for causing a computer to function as the reaction temperature calculation device described in any one of claims 5 to 8. A non-transitory computer-readable recording medium storing the program described in claim 9.