JP7262292B2 - Information provision method, pressure loss estimation calculation device, pressure loss estimation program, and non-temporary readable recording medium for computer - Google Patents

Description

Application of Article 30, Paragraph 2 of the Patent Act ・The 48th Petroleum and Petrochemical Symposium (60th Anniversary Commemorative Tokyo Conference) Lecture Summary, p.129, Date of issue: October 17, 2018 Petrochemical Symposium (60th Anniversary Commemorative Tokyo Conference), October 17, 2018 ・44th Refining Panel Discussion, February 22, 2019

TECHNICAL FIELD The present invention relates to an information providing method, a pressure loss estimation calculation device, a pressure loss estimation program, and a computer non-temporary readable recording medium.

Conventionally, a reaction method in which a gaseous and/or liquid reactant is passed through a reactor filled with a solid catalyst is known as a fixed bed flow reaction. In a fixed bed flow reactor, the flow of fluid containing the reactants is lost due to resistance from the solid catalyst bed. This loss is expressed in terms of pressure and is called pressure loss.

Usually, reactors used in fixed-bed flow-type reactions have a fixed upper limit of pressure resistance depending on the material, structure, etc., and it is necessary to constantly monitor the pressure inside the reactor so that the upper limit is not reached. be. The reaction must be stopped before the pressure inside the reactor reaches the upper limit of the pressure resistance of the reactor. In particular, when the pressure loss suddenly increases, the reaction may have to be stopped urgently, and in that case, the operation plan and the like will be greatly affected. Therefore, from the viewpoint of stable operation, there is a high need for a method of providing highly accurate pressure loss estimation values.

If the fluid contains impurities, the impurities may deposit on the solid catalyst layer. Also, if the fluid contains compounds with carbon elements, coke may form in the reactor and deposit on the solid catalyst layer. When impurities, coke, etc. accumulate in the solid catalyst layer, the pores of the solid catalyst layer are gradually clogged. This is considered to be one of the factors for the increase in pressure drop in the fixed bed flow reaction.

Ergun's equation is well known as one of the equations for calculating the pressure loss when the fluid is one phase of gas or liquid. The Ergun formula has a wide range of applications from laminar flow regions to turbulent flow regions, and has been widely used for a long time (Non-Patent Document 1). In addition, many formulas for calculating pressure loss when the Ergun formula is extended to a two-phase system of a gas and a liquid have been proposed, and one of such formulas is the Ergun-Larkins formula ( Non-Patent Document 2).

Ergun, S., Chem. Eng. Prog., 48-2 (1952), 89-94. R. P. LARKINS et al., "Two-Phase Concurrent Flow in Packed Beds", A. I. Ch. E. Journal, (1961) Vol. 7, No. 2, 231-239.

Both the Ergun equation and the Ergun-Larkins equation can be used to estimate the pressure drop by substituting necessary parameters such as the porosity of the solid catalyst layer in the reactor, the density of the fluid, the viscosity of the fluid, and the linear velocity of the fluid into the equation. is a formula for calculating

However, since it is difficult to acquire or estimate the above parameters from the reactor of the user plant over time, information indicating the estimated pressure loss is acquired over time by the Ergun formula, Ergun-Larkins formula, etc., practically impossible to provide.

The present invention has been made in view of the above circumstances, and an object of the present invention is to provide a method for providing a user terminal with information indicating an estimated value of pressure loss in a reactor of a user plant in a fixed bed flow reaction. do.

In order to solve the above problems, the present invention has the following aspects.
[1] A fixed-bed flow system in which an information processing device circulates a one-phase fluid of gas or liquid, or a two-phase fluid of gas and liquid from a user terminal to a reactor of a user plant in which a solid catalyst layer is formed. receiving over a network porosity estimation information and plant attribute information for the reaction;
a porosity calculation step in which the information processing device calculates the porosity of the solid catalyst layer in the reactor of the user plant using the solid catalyst layer porosity calculation function 1 based on the received porosity estimation information;
a pressure loss calculation step in which the information processing device calculates an estimated pressure loss value in the reactor of the user plant using a pressure loss estimation calculation function based on the porosity and the plant attribute information;
An information providing method, comprising: transmitting information indicating the calculated pressure loss estimated value to the user terminal.
[2] The porosity estimation information indicates information indicating the total amount of impurities in the fluid that has flowed into the reactor of the user plant during a certain period of time, and indicates the total amount of impurities in the fluid that has flowed out of the reactor of the user plant. The method of [1], comprising:
[3] The plant attribute information includes at least one type of information selected from the group consisting of information on properties of the fluid, information on the filling configuration of the solid catalyst, and information on the type of the solid catalyst. Or the method described in [2].
[4] The solid catalyst layer porosity calculation function 1 and the pressure loss estimation calculation function are calculated by an information processing device, in the initial stage of the reaction, in which the measured value of the pressure loss in the reactor, the porosity estimation information, and the plant attribute The method of any one of [1] to [3], using informedly calculated tuning parameters.
[5] The porosity estimation information includes information indicating the reaction temperature Tt _(x) of the solid catalyst layer, and the relationship between the _Tt(x) and the coking threshold T _B is such that _Tt(x) >T When _B is satisfied, in the porosity calculation step, instead of the solid catalyst layer porosity calculation function 1, the solid catalyst layer porosity calculation function 2 is used to calculate the porosity of the solid catalyst layer in the reactor of the user plant. The method according to any one of [1] to [4].
[6] The solid catalyst layer porosity _calculation function ₂ is used by the information processing device to perform _{the reaction} The method according to [5], wherein the tuning parameter calculated based on the measured value of the pressure loss in the vessel and the porosity estimation information and the plant attribute information is used.
[7] The method according to any one of [1] to [6], wherein the fixed-bed flow-type reaction is a hydrotreating reaction for heavy hydrocarbon oil or a hydrotreating reaction for light hydrocarbon oil.
[8] having a processor and storage means for storing computer readable instructions;
When the computer readable instructions are executed by the processor, a one-phase fluid of gas or liquid or a two-phase fluid of gas and liquid is passed from the user terminal to the reactor of the user plant in which the solid catalyst layer is formed. Receive via a network porosity estimation information and plant attribute information regarding the fixed bed flow reaction,
calculating the porosity of the solid catalyst layer in the reactor of the user plant by the solid catalyst layer porosity calculation function 1 based on the received porosity estimation information;
calculating an estimated pressure loss value in the reactor of the user plant by a pressure loss estimation calculation function based on the porosity and the plant attribute information;
A pressure loss estimation calculation device that transmits information indicating the calculated pressure loss estimation value to the user terminal.
[9] The porosity estimation information indicates information indicating the total amount of impurities in the fluid that flowed into the reactor of the user plant during a certain period, and indicates the total amount of impurities in the fluid that flowed out from the reactor of the user plant. The pressure loss estimation calculation device according to [8], including information.
[10] The plant attribute information includes at least one type of information selected from the group consisting of information on the properties of the fluid, information on the filling configuration of the solid catalyst, and information on the type of the solid catalyst, [8] Or the pressure loss estimation calculation device according to [9].
[11] The solid catalyst layer porosity calculation function 1 and the pressure drop estimation calculation function are calculated based on the measured value of the pressure loss in the reactor at the initial stage of the reaction, the porosity estimation information, and the plant attribute information. The pressure loss estimation calculation device according to any one of [8] to [10], which uses tuning parameters.
[12] The porosity estimation information includes information indicating the reaction temperature T _t(x) of the solid catalyst layer, and the relationship between the T _t(x) and the coking threshold T _B is such that T _t(x) >T When _B is satisfied, in the calculation of the porosity, instead of the solid catalyst layer porosity calculation function 1, the solid catalyst layer porosity calculation function 2 is used to calculate the porosity of the solid catalyst layer in the reactor of the user plant. The pressure loss estimation calculation device according to any one of [8] to [11], which calculates the pressure loss estimation calculation device.
[13] The solid catalyst layer porosity _calculation function 2 is such _that the pressure loss in _{the reactor} is The pressure loss estimation calculation device according to [12], which uses a tuning parameter calculated based on the measured value of and the porosity estimation information and the plant attribute information.
[14] The pressure drop according to any one of [8] to [13], wherein the fixed-bed flow-type reaction is a hydrotreating reaction for heavy hydrocarbon oil or a hydrotreating reaction for light hydrocarbon oil. Estimation calculator.
[15] A pressure loss estimation program for causing a computer to function as the pressure loss estimation calculation device according to any one of [8] to [14].
[16] A computer non-transitory readable recording medium storing the program according to [15].

According to the present invention, it is possible to provide a method of providing a user terminal with information indicating an estimated value of pressure loss in a reactor of a user plant in a fixed bed flow reaction.

It is a figure which shows the flow of the information provision method of this embodiment. It is a figure which shows the system configuration example of the information provision system 100. FIG.

Embodiments of the present invention will be described in detail below, but the following description is an example of the embodiments of the present invention, and the present invention is not limited to these contents, and can be modified within the scope of the gist thereof. can do.

<<Method of providing information indicating the estimated pressure loss value in the reactor of the user plant>>
The method of providing information indicating the estimated pressure loss value in the reactor of the user plant according to the present embodiment is such that the information processing device transmits gas or liquid from the user terminal to the reactor of the user plant in which the solid catalyst layer is formed. Receiving porosity estimation information and plant attribute information via a network (S1B and S1A in FIG. ), and a porosity calculation step (Fig. 1 S1B-1), and the information processing device calculates an estimated pressure loss value in the reactor of the user plant by a pressure loss estimation calculation function based on the porosity and the plant attribute information. It includes a calculating step (S2 in FIG. 1), and a step (S3 in FIG. 1) in which the information processing device transmits information indicating the calculated pressure loss estimated value to the user terminal.
The porosity calculation step and the pressure loss calculation step will be described in detail below.

<First Embodiment of Porosity Calculation Step>
The porosity calculation step of the present embodiment is a step of calculating the porosity of the solid catalyst layer in the reactor of the user plant by the solid catalyst layer porosity calculation function 1 based on the porosity estimation information received from the user terminal. be.
The solid catalyst layer porosity calculation function 1 in the present embodiment is based on the premise that impurities accumulated in the solid catalyst layer reduce the porosity of the solid catalyst layer. As such a solid catalyst layer porosity calculation function 1, for example, the following formula (1) is given.

In the above formula (1), ε _x is the porosity of the solid catalyst layer in the reactor at an arbitrary reaction lapse time t _x , and ε _x-1 is another arbitrary reaction lapse time before the reaction lapse time t _x . The porosity of the solid catalyst layer in the reactor at t _x-1 , S _IN is the total amount of impurities in the fluid that flowed into the reactor during a certain period from the reaction time t _x-1 to the reaction time t _x , S _OUT is the total amount of impurities in the fluid flowing out of the reactor during a certain period from the reaction lapse time t _x−1 to the reaction lapse time t _x , and α is a tuning parameter (constant).

That is, when the formula (1) is used as the solid catalyst layer porosity calculation function 1, the porosity estimation information preferably includes information on S _IN and S _OUT . ε _x−1 and α may be received from the user terminal or calculated by the information processing device as porosity estimation information. A method of calculating ε _x−1 and α will be described later.

(S _IN , S _OUT )
In the above formula (1), the total impurity amount S _IN in the fluid that has flowed into the reactor during a certain period (t _x -t _x-1 ) from the reaction lapse time t x _-1 to the reaction lapse time t _x , and ₍ S IN - S OUT ), which is the difference between the total amount of impurities S _OUT in the fluid flowing out of the reactor, the (S _{IN -} S _OUT ) amount of impurities is deposited on the solid catalyst layer, and the reactor It is thought that the porosity of the solid catalyst layer inside is reduced.
As used herein, "impurities" mean, for example, substances other than reactants of the target chemical reaction at the reactor inlet, and substances derived from "impurities" at the reactor inlet at the reactor outlet. Further, there is no need to measure substances such as nitrogen gas, which are generally thought to be inert in chemical reactions and not reduce the porosity of the solid catalyst layer. Impurities deposited on the solid catalyst layer may be appropriately selected according to the desired chemical reaction, and information on the impurities may be received.

S _IN and S _OUT are acquired in the user plant, and the information processing apparatus of the present embodiment receives them as porosity estimation information via the network, but the acquisition method in the user plant is not particularly limited. can be obtained by a known method in

An example of a method for obtaining S _IN and S _OUT in the user plant will be described below. _The S _IN is the _impurity concentration _{( unit} : (for example, ppm) is measured and calculated by calculating the product with the total amount (unit: kg) of the fluid that has flowed into the reactor during the predetermined period. Further, the S _OUT is the concentration of impurities in the fluid immediately after flowing out of the reactor during a certain period (t _x -t _x-1 ) from the reaction lapse time t _x-1 to the reaction lapse time t _x . (unit: ppm, for example), and calculate the product by the total amount (unit: kg) of the fluid that has flowed out of the reactor during the predetermined period.

As a method for measuring the concentration of impurities in a fluid, a method known in the art can be adopted depending on the type of impurity and fluid. Examples include various types of chromatography such as liquid chromatography and gas chromatography, and fluorescent X-ray analysis. The concentration of impurities in the fluid flowing into the reactor and the fluid flowing out of the reactor may be obtained in real time during the certain period of time, or may be obtained periodically or irregularly. In the case of regular or irregular acquisition, the acquisition may be performed once or more during the fixed period, and in the case of acquisition twice or more, the average value thereof can be used. Further, the acquisition of the impurity concentration may be performed manually and mechanically, or may be performed only by the machine (automation), but is preferably performed only by the machine if possible. The same applies to acquisition and control of other parameters, which will be described later.

The total amount of fluid that has flowed into the reactor and the total amount of fluid that has flowed out of the reactor during a certain period (t _x -t _{x -1} ) from the reaction lapse time t _x-1 to the reaction lapse time t x is the flow rate It can be obtained by the liquid level change of the meter, the raw material tank and the product tank, and the like. In addition, the total amount of fluid flowing into the reactor and the total amount of fluid flowing out of the reactor during a certain period (t _x −t _x − _{1 ) from the reaction lapse time t x −1} to the reaction lapse time t x are A desired amount can be obtained by controlling with a mass flow controller, control valve, pump, compressor, or the like.

(ε _x−1 )
The porosity ε _x-1 of the solid catalyst layer in the reactor at the reaction elapsed time t _x-1 in the above formula (1) is, for example, at another arbitrary reaction elapsed time before the reaction elapsed time t _x-1 The porosity ε _x-2 of the solid catalyst layer in the reactor at t _x-2 , and the fluid flowing into the reactor during a certain period from the reaction time t _x-2 to the reaction time t _x-1 can be calculated by substituting the total amount of impurities S _IN and the total amount of impurities S _OUT in the fluid discharged from the reactor into the above equation (1). That is, if _ε0 , which is the porosity of the solid catalyst layer in the reactor at the start of the reaction, is known, then by repeatedly applying the above equation (1), the voids of the solid catalyst layer in the reactor can be The change in rate ε over time can be obtained.

ε ₀ is acquired at the user plant, and the information processing apparatus of the present embodiment receives it via the network before the reaction starts. can be obtained by

An example of a method for obtaining _ε0 in the user plant will be described below. The porosity ε ₀ of the solid catalyst layer in the reactor at the start of the reaction is, for example, the packing density BD (unit: kg/m ³ ) of the solid catalyst layer, the true density ρ _cat ( The unit is, for example, kg/m ³ ), and the pore volume PV of the packed solid catalyst (the unit is, for example, m ³ /kg) are measured, respectively, and ε ₀ =1−(BD×(1/ρ _cat +PV )) can be obtained by calculating

The packing density BD of the solid catalyst layer is BD=W _cat /V cat from the packing volume V cat (unit is m ³ ) of the solid catalyst layer and the packing weight W _cat (unit is kg) of the solid catalyst _{layer .} can be obtained by calculating
The packed volume V _cat of the solid catalyst layer is obtained by multiplying the layer height of the solid catalyst layer (unit: m) by the cross-sectional area of the reactor (eg, cylindrical tubular reactor) (unit: m ² ). can be obtained by A method for measuring the layer height of the solid catalyst layer will be described later.
The true density ρ _cat of the solid catalyst can be measured by a method known in the art, and can be obtained, for example, by measurement using a pycnometer method. The pycnometer method is a measurement method based on Archimedes' principle, and there are a liquid phase method and a gas phase method as measurement means.
The pore volume PV of the solid catalyst can be obtained by a mercury intrusion method or a gas (nitrogen gas or the like) adsorption method.

When a plurality of different solid catalyst layers are formed in the reactor, in the porosity calculation step of this embodiment, the solid porosity calculation function 1 represented by the following formula (1-A) is used to calculate the user plant The porosity of the solid catalyst layer in the reactor may be calculated (ε _x(n) calculation method (1)).

In the formula (1-A), n is an integer of 2 or more and represents the number of different solid catalyst layers. ε _x(n) is the porosity of the n-th solid catalyst layer from the reactor inlet side at the reaction time t _x , and ε _x−1(n) is the reactor at the reaction time t _x−1 The porosity of the n-th solid catalyst layer from the inlet side, α _(n) is the tuning parameter of the n-th solid catalyst layer from the reactor inlet side, and R _(n) is the n-th layer from the reactor inlet side. The sum of R ₍₁₎ to R _(n) is one. S _IN and S _OUT are the same as above.

The solid catalyst layer ratio R _(n) is the total amount of impurities in the fluid that has flowed into the reactor during a certain period (t _x -t _x-1 ) from the reaction lapse time t _x-1 to the reaction lapse time t _x Among the difference between S _IN and the total amount of impurities S _OUT in the fluid flowing out of the reactor (S _IN −S _OUT ), the amount deposited on each of the plurality of different solid catalyst layers is proportionally divided. is a coefficient for

When a plurality of different solid catalyst layers are formed in the reactor, in the porosity calculation step of this embodiment, the solid porosity calculation function 1 represented by the following formula (1-B) is used to calculate the reaction of the user plant The porosity of the solid catalyst layer in the vessel may be calculated (ε _x(n) calculation method (2)).

In the formula (1-B), n is an integer of 2 or more and represents the number of different solid catalyst layers. ε _x(n) is the porosity of the n-th solid catalyst layer from the reactor inlet side at the reaction time t _x , and ε _x−1(n) is the reactor at the reaction time t _x−1 The porosity of the n-th solid catalyst layer from the inlet side, α _const , is a tuning parameter, and S _IN and S _OUT are the same as above. In the ε _x(n) calculation method (2), the same α _const is used in calculating the porosity of each of the n solid catalyst layers, and the solid catalyst layer ratio is not used _{. n)} The porosity of the solid catalyst layer can be obtained more easily than the calculation method (1).

<Second Embodiment of Porosity Calculation Step>
In the porosity calculation step of the present embodiment, the porosity estimation information includes information indicating the reaction temperature Tt _(x) of the solid catalyst layer, and the relationship between the Tt _(x) and the coking threshold T _B is _Tt When _(x) >T _B is satisfied, in the porosity calculation step, instead of the solid catalyst layer porosity calculation function 1, the solid catalyst layer porosity calculation function 2 is used to calculate the solid catalyst layer in the reactor of the user plant. This is a step of calculating the porosity of
In the solid catalyst layer porosity calculation function 2 in the present embodiment, it is assumed that impurities accumulated in the solid catalyst layer and coke generated in the reaction reduce the porosity of the solid catalyst layer. As such a solid catalyst layer porosity calculation function 2, for example, the following formula (1-1) is given.

In the above formula (1-1), T _{t (x)} is the reaction temperature of the solid catalyst layer at the reaction elapsed time t _x , T _B is the coking threshold (constant), R is the gas constant, β, γ are the tuning parameters ( constant). ε _x , ε _x−1 , α, S _IN , and S _OUT are the same as in the above formula (1).

When the formula (1-1) is used as the solid catalyst layer porosity calculation function 2, the porosity estimation information preferably includes information on S _IN , S _OUT , and T _t(x) . It is preferable that _TB is obtained in advance by a method described later and set in the information processing apparatus. Also, ε _x−1 , α, β, and γ may be received from the user terminal as porosity estimation information, or may be calculated by the information processing device. The method for calculating ε _x−1 is as described above. A method for obtaining α, β, and γ will be described later.

(T _t(x) )
The reaction temperature Tt _(x) of the solid catalyst layer at the reaction elapsed time _tx is acquired at the user plant, and the information processing apparatus of the present embodiment receives it as porosity estimation information via the network. The acquisition method is not particularly limited, and it can be acquired by a method known in this field.

Examples of the reaction temperature T _{t (x)} at the time t _x of the reaction progress include the maximum temperature of the solid catalyst layer (hot spot temperature), the weight average temperature of the solid catalyst layer (WABT), the inlet temperature of the reactor, and the outlet of the reactor. Examples include the temperature, the average temperature of the inlet temperature of the reactor and the outlet temperature of the reactor, etc. Among them, it is preferable to adopt the maximum temperature of the solid catalyst layer. The above temperatures can be obtained, for example, with a thermometer or the like in the reactor.

( _TB )
In the above formula (1-1), the coking threshold T _B is the temperature at which coke is generated and starts depositing on the solid catalyst layer. The coking threshold is uniquely determined given the type of solid catalyst, the type of fluid containing the reactants, and the combination of liquid hourly space velocity (LHSV) and/or gas hourly space velocity (GHSV) of said fluid relative to said solid catalyst. be done. That is, when the above combination is determined, _TB becomes a constant value. A method for obtaining the coking threshold T _B will be described below, but this method is an example, and the method for obtaining T _B is not limited to this.

(T _B acquisition method 1)
As described above, the coking threshold T _B is the temperature at which coke forms and begins to deposit on the solid catalyst layer. Therefore, in the case of a reaction in which the solid catalyst can be extracted over time, the extracted solid catalyst is analyzed by elemental analysis, etc., and the reaction temperature when the carbon concentration in the solid catalyst exceeds a certain value is determined. can be _TB . The constant value is, for example, 0.05% by mass or more. Extraction of the solid catalyst and elemental analysis are preferably carried out at intervals of 5 to 20°C, more preferably at intervals of 5 to 10°C. The reaction temperature is as explained above, and it is preferable to adopt the maximum temperature of the solid catalyst layer.
In this method, the coking threshold T _B may be obtained while reacting in a user plant (actual equipment), or may be obtained in advance in a laboratory or bench scale that is smaller than the actual equipment. When obtaining the coking threshold _TB in advance on a lab or bench scale, as described above, the type of solid catalyst, the type of fluid containing reactants, and the LHSV and / or GHSV of the fluid with respect to the solid catalyst are measured on the actual machine. The reaction conditions may be the same as those of .
In an actual machine, it is often difficult to extract the catalyst over time. Therefore, in method 1 for obtaining the coking threshold _TB , it is preferable to obtain the coking threshold _TB in advance on a laboratory or bench scale. .

(T _B acquisition method 2)
As described above, when coke starts to form, the coke begins to deposit on the solid catalyst layer, gradually clogging the pores of the solid catalyst layer and increasing the pressure loss. In fixed-bed flow-type reactions, the activity of solid catalysts decreases over time due to various factors, so the reaction is carried out while increasing the reaction temperature over time in order to keep the activity of the reactor as a whole constant.
In the hydrotreatment reaction of heavy hydrocarbon oil, which is a fixed-bed flow reaction in which two-phase fluids of gas and liquid flow, plotting the measured value of the pressure drop in the reactor against the reaction temperature shows that coke is generated. A linear relationship (straight line 1) represented by y=a ₁ x+b ₁ is obtained from the beginning of the reaction to the middle stage of the reaction when the solid catalyst layer is not deposited. In the straight line 1, y is the measured pressure drop in the reactor, x is the reaction temperature, _a1 is the slope, and _b1 is the intercept. The reaction temperature is as explained above, and it is preferable to adopt the maximum temperature of the solid catalyst layer.

When plotting the measured value of the pressure loss in the reactor against the reaction temperature in the middle to late reaction period when coke starts to deposit on the solid catalyst layer, the plot deviates greatly from the straight line 1 above.
Then, when plotting the measured value of the pressure loss in the reactor against the reaction temperature in the middle to the late reaction period when coke started to deposit on the solid catalyst layer, a new straight line represented by y = a ₂ x + b ₂ was obtained. A relationship (straight line 2) is obtained. In the straight line 2, y is the measured value of the pressure loss in the reactor, x is the reaction temperature, _a2 is the slope and satisfies _a2 > _a1 , and _b2 is the intercept and satisfies _b2 < _b1 .
That is, in the hydrotreatment reaction of heavy hydrocarbon oil, which is a fixed-bed flow reaction in which two-phase fluids of gas and liquid flow, the measured value of the pressure loss in the reactor was plotted against the reaction temperature. Sometimes, the plot shifts from the straight line 1 to the straight line 2 before and after the start of deposition of coke on the solid catalyst layer, and at the intersection of the straight lines 1 and 2 (point of inflection from straight line 1 to straight line 2) The reaction temperature can be _TB .

A method for obtaining the inflection point will be specifically described. From the start of the reaction, the measured value of the pressure loss in the reactor and the reaction temperature are acquired over time, plotted, and the straight line 1 is obtained using calculation software such as Excel. For example, the above plotting is performed at M points from the start of the reaction to obtain a straight line 1 represented by y=a ₁ x+b ₁ . M is a positive integer, for example 5-350. Subsequently, the reaction temperature at the M+1th point is substituted for x in the equation of straight line 1 to obtain y _(M+1) . ΔP _(M+1) /y (M+1), which is the ratio of the obtained y ₍ M+1) and the measured value ΔP _{(M+1) of} the pressure loss in the reactor at the M+1th point, is calculated.
When the ΔP _(M+1) /y _(M+1) is 0.8 to 1.2, the plot is determined as on the straight line 1, and a ₁ and b ₁ of the straight line 1 are recalculated by adding the plot. After the M + 2nd point, the ratio between the calculated value and the measured value of the pressure loss in the reactor is similarly calculated. It is processed in the same way as for points.

When the ratio exceeds 1.2, coke is generated, the coke begins to deposit on the solid catalyst layer, and the plot of the measured value of pressure loss in the reactor against the reaction temperature changes from the straight line 1 to the straight line 2 It can be determined that the transition to At N points after the point where the ratio exceeds 1.2, the measured value of the pressure loss in the reactor and the reaction temperature are obtained over time, plotted, and represented by y = a ₂ x + b ₂ A straight line 2 is obtained using excel or the like. N is a positive integer, eg 5-350.
Then, the intersection of the straight lines 1 and 2 is obtained, and the coking threshold T _B can be obtained as x at the intersection.
In this method, the coking threshold T _B may be obtained while reacting in a user plant (actual equipment), or may be obtained in advance in a laboratory or bench scale that is smaller than the actual equipment. When obtaining the coking threshold _TB in advance on a lab or bench scale, as described above, the type of solid catalyst, the type of fluid containing the reactant, and the LHSV and / or GHSV of the fluid with respect to the solid catalyst are measured with an actual machine. The reaction conditions may be the same as those of .

Method 2 for obtaining the threshold value _TB for coking is preferable to method 1 for obtaining the threshold value _TB for coking in that the solid catalyst does not need to be extracted and the reaction does not need to be stopped.

When a plurality of different solid catalyst layers are formed in the reactor, in the porosity calculation step of the present embodiment, [ε _x−1 −α(S _IN −S _OUT )] may be calculated for each catalyst layer as in the above formulas (1-A) and (1-B) to calculate the porosity of each catalyst layer.

<Pressure loss calculation step>
In the pressure loss calculation step of the present embodiment, the pressure loss in the reactor of the user plant is calculated by the pressure loss estimation calculation function based on the porosity calculated in the porosity calculation step and the plant attribute information received from the user terminal. This is the step of calculating the estimated value. The pressure loss estimation calculation function is composed of a pressure loss calculation function and a correction function for each reactor. Specifically, based on the plant attribute information, the pressure loss calculation value is calculated by the pressure loss calculation function, and the pressure loss estimated value is calculated by the correction function for each reactor based on the obtained pressure loss calculation value. .
Hereinafter, the pressure loss calculation function and the correction function for each reactor will be described in detail with examples.

<Pressure loss calculation function>
As the pressure loss calculation function, a formula known in the art that can calculate the pressure loss calculation value based on either or both of the porosity of the solid catalyst layer in the reactor and the plant attribute information is used. can be done. Examples of the pressure loss calculation function when the fluid is one phase of gas or liquid include Ergun formula, Blake-Kozeny formula, Burke-Plummer formula, Kozeny-Carman formula, and Fanning formula. Examples of functions for calculating the pressure loss in the reactor in the case of two phases include the Ergun-Larkins formula and the Lockhart-Martinelli formula, but are not limited to these.

The plant attribute information is parameters other than the porosity of the solid catalyst layer necessary for calculating the pressure loss calculation value by the pressure loss calculation function, and includes information on the properties of the fluid and information on the filling configuration of the solid catalyst. , and information about the type of solid catalyst.

(Properties of fluid)
Examples of the information about the property of the fluid include information about the viscosity of the fluid, information about the linear velocity of the fluid, and information about the density of the fluid.

(Filling structure of solid catalyst)
Examples of the information on the packing configuration of the solid catalyst as the plant attribute information include information on the number of packed solid catalyst layers and information on the layer height of each of the solid catalyst layers.

(Type of solid catalyst)
Information on the type of solid catalyst as plant attribute information includes, for example, information on the composition of the solid catalyst and information on the shape of the solid catalyst.

Hereinafter, the Ergun formula is used as the pressure loss calculation function in the reactor when the fluid is gas or liquid in one phase, and the Ergun-Larkins formula is used as the pressure loss calculation function in the reactor when the fluid is gas and liquid in two phases. However, the present invention is not limited to these formulas.

<Ergun formula>
In the fixed bed flow reaction, the calculated value of pressure loss in the reactor when the fluid is one phase of gas or liquid can be calculated by Ergun's formula represented by the following formula (2). In this embodiment, the calculated value of the pressure loss in the reactor determined by the Ergun equation is expressed as ΔP1 _cal .

In the above formula (2), a, b, and m are constants in the Ergun equation, ε is the porosity of the solid catalyst layer in the reactor, μ is the viscosity of the fluid [kg/ms], u is the linear velocity of the fluid [m /s], ρ is the density of the fluid [kg/m ³ ], dp is the sphere diameter [m] when the solid catalyst is assumed to be a sphere, and H is the bed height of the solid catalyst [m].

a, b, and m in the above formula (2) are constants, and are empirically obtained values. When the solid catalyst is spherical, if a=150, b=1.75, and m=3.0, the pressure loss calculated value can be calculated with high accuracy. When the solid catalyst is not spherical, a=180, b=1.80, and m=3.6 make it possible to calculate the pressure loss calculation value with high accuracy.

In the present embodiment, the porosity calculated by the porosity calculating step is used as ε in the formula (2).

μ is the viscosity of the fluid at the reaction temperature [kg/ms], ρ is the density of the fluid at the reaction temperature [kg/m ³ ], u is the linear velocity of the fluid at the reaction temperature [m/s], These pieces of information are included in the information regarding the properties of the fluid.

μ, ρ, and u are acquired at the user plant, and the information processing apparatus of the present embodiment receives them as information on the properties of the fluid via the network, but the method of acquisition at the user plant is not particularly limited, It can be obtained by a method known in this field.

dp is the sphere diameter [m] when the solid catalyst is assumed to be a sphere, and this information is included in the information on the type of solid catalyst.

dp is acquired in the user plant, and the information processing device of the present embodiment receives it as information on the type of solid catalyst via the network, but the acquisition method in the user plant is not particularly limited, and is known in the art. It can be obtained by the method.

An example of a method for obtaining dp in the user plant will be described below. The shape of the solid catalyst used in the fixed-bed flow-type reaction is selected according to its application. catalyst geometry is often used.

In this embodiment, if the filled solid catalyst is spherical, the diameter of the sphere can be dp. On the other hand, when the solid catalyst is not spherical, the diameter of the sphere can be determined assuming that the solid catalyst is a sphere, and the diameter can be defined as dp. As described in known literature (Ind. Eng. Chem. Des. Dev. 1986, 25, 1034-1036), for example, formula (3-1) for a cylinder, formula (3-2) for a trefoil type , in the case of a four-leaf type, it can be obtained by the formula (3-3).

In the above formulas (3-1) to (3-3), L is the average major axis [m] of the solid catalyst, and D is the average minor axis [m] of the solid catalyst. For the average major axis and average minor axis of the solid catalyst, for example, the major axis and minor axis of 50 or more solid catalysts are measured, and the average value can be adopted.
In this embodiment, the information processing device preferably receives the dp of the solid catalyst via the network before starting the reaction. It can be a constant value.

H is the layer height [m] of the solid catalyst layer, and this information is included in the information about the packing configuration of the solid catalyst.

H is acquired at the user plant, and the information processing device of the present embodiment receives it via the network as information on the filling configuration of the solid catalyst. can be obtained by the method of

An example of a method for obtaining H in the user plant will be described below. Said H can be measured by measuring, for example, when the reactor is filled with the solid catalyst before the reaction.
In this embodiment, the information processing device preferably receives the layer height of the solid catalyst via the network before starting the reaction. can be a constant value.

The pressure loss calculated value ΔP1 _cal can be calculated by substituting the above parameters into the equation (2).

<Ergun-Larkins formula>
In a fixed bed flow reaction, the calculated value of pressure loss in the reactor when the fluid is two phases of gas and liquid can be calculated by the Ergun-Larkins formula consisting of the following formulas (4) to (9). can. In this embodiment, the calculated value of the pressure loss in the reactor determined by the Ergun-Larkins formula is denoted as ΔP2 _cal .

In the above formula (4), _δL is the liquid ΔP _cal /H, _δG is the gas ΔP _cal /H, _δLG is the gas-liquid ΔP _cal /H, and χ=( _δL / _δG ) ^{1 /2} and 0.05<χ<30. )

In equation (5) above, _RL is the liquid holdup.

In the above formula (6), _ρm is the gas-liquid average density, _ρL is the liquid density, _ρG is the gas density, and _RL is the same as above.

Calculation of the pressure loss calculated value ΔP2 _cal in the reactor by the Ergun-Larkins formula will be described below.
First, _δL and _δG are calculated by the Ergun formula as follows (formula (8) and formula (9) below).

In the above formula (8), a, b, and m are constants in the Ergun equation, ε is the porosity of the solid catalyst layer in the reactor, μ _L is the viscosity of the liquid [kg/ms], and u _L is the linear velocity of the liquid. [m/s], ρ _L is the density of the liquid [kg/m ³ ], dp is the sphere diameter [m] when the solid catalyst is assumed to be a sphere, and H is the layer height of the catalyst [m]. These values are as described in the Ergun formula.

In the present embodiment, the porosity calculated by the porosity calculating step is used as ε in the formula (8).

In the above formula (9), a, b, and m are constants in the Ergun formula, ε is the porosity of the solid catalyst layer in the reactor, μ _G is the viscosity of the gas [kg/ms], and u _G is the linear velocity of the gas. [m/s], _ρG is the density of the gas [kg/m ³ ], dp is the sphere diameter [m] when the solid catalyst is assumed to be a sphere, and H is the layer height of the catalyst [m]. These values are as described in the Ergun formula.

In this embodiment, the porosity calculated by the porosity calculating step is used as ε in the formula (9).

χ=( _δL / _δG ) ^1/2 is calculated from the obtained _δL and _δG . Subsequently, using δ _L , δ _G , and χ, δ _LG is calculated from the above equation (4), and R _L is calculated from the above equation (5). Subsequently, using the obtained _RL , _ρm is calculated from the above equation (6). Using the obtained δ _LG and ρ _m , the pressure loss calculated value ΔP2 _cal can be calculated from the above equation (7).

<<Correction function for each reactor>>
The correction function for each reactor is a function for correcting the pressure loss derived from the structure of each reactor other than the pressure loss due to the solid catalyst layer.
As the correction function for each reactor, for example, the following formula (10) is given.

In the above equation (10), ΔP _sim is an estimated pressure loss value, ΔP _cal is a calculated pressure loss value, and σ is a tuning parameter (constant). σ may be received from a user terminal as plant attribute information, or may be calculated by an information processing device. A method for calculating σ will be described later.

σ is a different value for each reactor, and represents the pressure loss due to the structure of the reactor other than the pressure loss due to the solid catalyst layer. That is, when the reaction is performed in a multi-tubular reactor, it is preferable to obtain σ for each reaction tube. The pressure loss estimated value ΔP _sim can be calculated by substituting the pressure loss calculated value ΔP _cal obtained by the pressure loss calculation function described above into the equation (10).

When a plurality of different solid catalyst layers are formed in the reactor, the pressure loss calculated value ΔP _cal(n) in each solid catalyst layer is calculated by the method described above, and by summing them, the total solid A calculated catalyst layer pressure loss value ΔP _cal can be obtained. Then, by substituting the obtained ΔP _cal into the above equation (10), it is possible to obtain the estimated pressure loss value ΔP _sim in the reactor when a plurality of different solid catalyst layers are formed in the reactor. can.

ΔP _sim calculated by the pressure loss calculation step of the present embodiment is ΔP/ΔP _sim on average of 0.50 or more and 1.50 or less when ΔP is the measured value of the pressure loss in the reactor. Preferably, it is more preferably 0.80 or more and 1.20 or less. An average of ΔP/ΔP _sim can be obtained, for example, by measuring ΔP/ΔP _sim at 15 or more points.

In the porosity calculation step, when only the solid catalyst layer porosity calculation function 1 is used (that is, when the solid catalyst layer porosity calculation function 2 is not used), the average value of ΔP/ΔP _sim in a predetermined period is within the above range. is deviated from, it is preferable to reset the tuning parameter α. If the average value of ΔP/ΔP _sim in the predetermined period is outside the above range, it means that the cause of the increase in pressure loss is not only deposition of impurities in the fluid on the solid catalyst layer but also other factors. It suggests A method of resetting the tuning parameter α will be described later.

<Calculation of tuning parameters 1>
A method of calculating the tuning parameter α in the above equation (1) and the tuning parameter σ in the above equation (10) will be described below. These tuning parameters can be calculated based on the measured value of the pressure loss in the reactor of the user plant, the porosity estimation information, and the plant attribute information at the initial stage of the reaction.

(Calculation 1 of tuning parameters α and σ)
When a single solid catalyst layer is formed in the reactor, the tuning parameter α in the formula (1) and the tuning parameter σ in the formula (10) can be set, for example, by the following method (α , σ setting method 1).
Based on the porosity estimation information and the plant attribute information, the pressure loss estimated value ΔP _sim in the reactor at an arbitrary reaction time t _x at the beginning of the reaction is calculated by the above formula (1), the pressure loss calculation function, and the above formula (10). Calculated by At this time, since α and σ are not fixed, ΔP _sim is a function of α and σ.
The values of α and σ can be set so that the relationship between the measured value ΔP of the pressure loss at the reaction elapsed time _tx and the ΔP _sim is ΔP=ΔP _sim .
As used herein, the term “initial stage of the reaction” means, for example, that V _flow /V _cat is the ratio of the total volume of the fluid that has flowed in from the start of the reaction (V _flow ) to the filling volume of the solid catalyst layer (V _cat ) is 100. It means the elapsed reaction time such that:

When a plurality of different solid catalyst layers are formed in the reactor and the porosity ε _x(n) of each solid catalyst layer is calculated by the ε _x(n) calculation method (2), the formula (1- The tuning parameter α _const in B) and the tuning parameter σ in Equation (10) can be set, for example, by the following method (α _const , σ setting method 1).
Based on the porosity estimation information and plant attribute information, the calculated pressure loss ΔP _cal(n) of each solid catalyst layer in the reactor at an arbitrary reaction time t _x at the beginning of the reaction is calculated by the above formula (1-B), the pressure It is calculated using a loss calculation function (n is an integer of 2 or more and represents the number of different solid catalyst layers; the same applies hereinafter). Then ΔP _cal(n) is a function of α _const . Subsequently, the pressure drop calculation value ΔP _{cal (n)} of each solid catalyst layer is summed up to obtain the pressure drop calculation value ΔP _cal of all solid catalyst layers as a function of α _const . The pressure loss calculated value ΔP _cal of the all-solid catalyst layer thus obtained is substituted into the above equation (10) to calculate the pressure loss estimated value ΔP _sim of the all-solid catalyst layer. At this time, since α _const and σ are not fixed, ΔP _sim is a function of α _const and σ.
The values of α _const and σ can be set so that the relationship between the measured value ΔP of the pressure loss at the reaction elapsed time t _x and the ΔP _sim is ΔP=ΔP _sim .

Preferably, the estimated pressure drop ΔP _sim and the measured pressure drop ΔP are compared over a plurality of reaction lapses to determine tuning parameters α(α _const ) and σ. For example, the ΔP _sim and the ΔP are obtained at arbitrary 15 or more reaction points, and the respective average values ΔP _{sim (ave)} and the ratio of ΔP (ave) ΔP _{(ave )} / ΔP _{sim (ave)} α(α _const ), σ can be set so that the value of is closest to unity.

(Calculation 2 of Tuning Parameters α and σ)
When a single solid catalyst layer is formed in the reactor, the tuning parameters α and σ may be set by the following method (method 2 for setting α and σ).
An estimated pressure loss value ΔP _sim in the reactor at an arbitrary reaction elapsed time t _int in the initial stage of the reaction is calculated from the pressure loss calculation function and Equation (10) based on the plant attribute information. At this time, as the porosity of the solid catalyst layer in the reactor, the above-described porosity _ε of the solid catalyst layer in the reactor at the start of the reaction is used. In this case, ΔP _sim is a function of σ.
The value of σ can be set so that the relationship between the measured value ΔP of the pressure loss at the reaction elapsed time t _int and the ΔP _sim is ΔP=ΔP _sim .

The porosity of the solid catalyst layer in the reactor at the above reaction time t _int is assumed to be ε ₀ , and the estimated pressure loss value ΔP _sim in the reactor at an arbitrary reaction time t _x after the initial reaction time t _int is Based on the porosity estimation information and the plant attribute information, it is calculated from the above equation (1), the pressure loss calculation function, and the above equation (10). At this time, σ is already determined, so ΔP _sim is a function of α.
The value of α can be set so that the relationship between the measured value ΔP of the pressure loss at the reaction elapsed time _tx and the ΔP _sim is ΔP=ΔP _sim .
At the beginning of the reaction, almost no impurities are deposited on the solid catalyst layer. Therefore, by using _ε0 as the porosity of the solid catalyst layer in the reactor approximately, σ and α are changed step by step, and can be uniquely determined.

When a plurality of different solid catalyst layers are formed in the reactor and the porosity ε _x(n) of each solid catalyst layer is calculated by the ε _x(n) calculation method (2), the formula (1- The tuning parameter α _const in B) and the tuning parameter σ in the above equation (10) may be set by the following method (method 2 for setting α _const and σ).
A pressure loss calculation value ΔP _cal(n) of each solid catalyst layer in the reactor at an arbitrary reaction time t _int in the initial stage of the reaction is calculated by a pressure loss calculation function based on the plant attribute information. At this time, the porosity ε _0(n) of each solid catalyst layer in the reactor at the start of the reaction is used as the porosity of each solid catalyst layer in the reactor. Subsequently, the pressure drop calculation value ΔP _cal of all solid catalyst layers is obtained by totaling the pressure drop calculation values ΔP _cal(n) of each solid catalyst layer. The pressure loss calculated value ΔP _cal of the all-solid catalyst layer thus obtained is substituted into the above equation (10) to calculate the pressure loss estimated value ΔP _sim of the all-solid catalyst layer. In this case, ΔP _sim is a function of σ.
The value of σ can be set so that the relationship between the measured value ΔP of the pressure loss at the reaction elapsed time t _int and the ΔP _sim is ΔP=ΔP _sim .

Assuming that the porosity of each solid catalyst layer in the reactor at the reaction time t _int is ε _{0 (n), the porosity} of each solid catalyst layer in the reactor at an arbitrary reaction time t _x after the initial reaction time t _int The calculated pressure loss value ΔP _cal(n) is calculated from the above formula (1-B) and the pressure loss calculation function based on the porosity estimation information and the plant attribute information. Then ΔP _cal(n) is a function of α _const . Subsequently, the pressure drop calculation value ΔP _{cal (n)} of each solid catalyst layer is summed up to obtain the pressure drop calculation value ΔP _cal of all solid catalyst layers as a function of α _const . The pressure loss calculated value ΔP _cal of the all-solid catalyst layer thus obtained is substituted into the above equation (10) to calculate the pressure loss estimated value ΔP _sim of the all-solid catalyst layer. At this time, σ is already determined, so ΔP _sim is a function of α _const .
The value of α _const can be set so that the relationship between the measured value ΔP of the pressure loss at the reaction elapsed time _tx and the ΔP _sim is ΔP=ΔP _sim .

When the reaction is performed in a shell-and-tube reactor having a plurality of reactors, it is preferable to calculate the tuning parameters α(α _const ) and σ for each reactor.

(Reset tuning parameter α)
In the porosity calculation step, when only the solid catalyst layer porosity calculation function 1 is used (that is, when the solid catalyst layer porosity calculation function 2 is not used), the tuning parameter α should be reset as follows. can be done.
Based on the porosity estimation information and the plant attribute information, the estimated pressure loss value ΔP _sim in the reactor at an arbitrary reaction time t _x after the average value of ΔP / ΔP _sim in a predetermined period is out of the specific range, It is calculated from the formula (1), the pressure loss calculation function, and the formula (10). At this time, the value of α may be reset such that the relationship between the measured value ΔP of the pressure loss at the reaction elapsed time _tx and the ΔP _sim is ΔP=ΔP _sim .

When a plurality of different solid catalyst layers are formed in the reactor and the porosity ε _x(n) of each solid catalyst layer is calculated by the ε _x(n) calculation method (2), ΔP/ When the average value of ΔP _sim is out of the range, it is preferable to reset the tuning parameter α _const as follows.
Calculated pressure loss ΔP _cal(n) of each solid catalyst layer in the reactor at arbitrary reaction time t _x after the average value of ΔP / ΔP _sim in a predetermined period is out of the specific range Estimate porosity Based on the information and plant attribute information, it is calculated by the above formula (1-B) and the pressure loss calculation function. Subsequently, the pressure drop calculation value ΔP _cal of all solid catalyst layers is obtained by totaling the pressure drop calculation values ΔP _cal(n) of each solid catalyst layer. The pressure loss calculated value ΔP _cal of the all-solid catalyst layer thus obtained is substituted into the above equation (10) to calculate the pressure loss estimated value ΔP _sim of the all-solid catalyst layer. At this time, the value of α _const may be reset so that the relationship between the measured value ΔP of the pressure loss at the reaction elapsed time _tx and the ΔP _sim is ΔP=ΔP _sim .

Comparison between the estimated pressure loss value ΔP _sim and the measured pressure loss value ΔP after the average value of ΔP/ΔP _sim in a predetermined period is out of the range is performed during a plurality of reactions, and tuning parameter α (α _const ) is preferably redetermined. For example, after the average value of ΔP / ΔP _sim in a predetermined period is outside the range, the ΔP _sim and the ΔP are obtained at any 15 or more reaction points, and the average value of each ΔP _{sim (ave )} , α ₍ α _const ) can be reset such that the value of the ratio ΔP _(ave) /ΔP _sim(ave) of ΔP (ave) is closest to unity.

<Calculation of tuning parameters 2>
A method of calculating the tuning parameters β and γ in the formula (1-1) will be described below. Note that the tuning parameter α calculated in <Tuning Parameter Calculation 1> can be used as it is for the tuning parameter α in the formula (1-1). Further, the tuning parameter σ calculated in <Tuning Parameter Calculation 1> can be used as it is for the tuning parameter σ in the formula (10).
The tuning parameters β and γ can be calculated based on the measured value of pressure loss in the reactor of the user plant, porosity estimation information, and plant attribute information.

(Calculation of tuning parameters β and γ 1)
Estimated pressure drop ΔP _sim in the reactor at an initial arbitrary reaction course t _x after the relationship between the reaction temperature T _t(x) and the coking threshold T _B satisfies T _t(x) >T _B for the first time is calculated by the formula (1-1), the pressure loss calculation function, and the formula (10) based on the porosity estimation information and the plant attribute information. At this time, since β and γ are not fixed, ΔP _sim is a function of β and γ.
The values of β and γ can be set so that the relationship between the measured value ΔP of the pressure loss at the reaction elapsed time _tx and the ΔP _sim is ΔP=ΔP _sim .
In the present specification, the term "initial period after T _t(x) >T _B is satisfied for the first time" is, for example, the period from when T _t(x) >T _B is satisfied for the first time to the time when the reaction of 15 points has elapsed. means For example, if the pressure drop estimate is calculated every other day, the "initial period after T _t(x) >T _B is first satisfied" is 15 days from the time when T _t(x) >T _B is first satisfied. becomes. However, in this specification, the interval for calculating the pressure loss estimated value is not limited to one day as described above, and may be any period.

The comparison between the estimated pressure loss value ΔP _sim and the measured pressure loss value ΔP is performed after the relationship between the reaction temperature T _t(x) and the coking threshold T _B satisfies T _t(x) >T _B for the first time. It is preferable to determine the tuning parameters β and γ at multiple reaction lapses after the initial reaction lapse time _tx . For example, the ΔP _sim and the ΔP are obtained at arbitrary 15 or more reaction points, and the respective average values ΔP _{sim (ave)} and the ratio of ΔP (ave) ΔP _{(ave )} / ΔP _{sim (ave)} β and γ can be set so that the value of is closest to one.

(Setting method 2 for tuning parameters β and γ)
Estimated pressure drop ΔP _sim in the reactor at an initial arbitrary reaction course t _x after the relationship between the reaction temperature T _t(x) and the coking threshold T _B satisfies T _t(x) >T _B for the first time is calculated by the formula (1-1), the pressure loss calculation function, and the formula (10) based on the porosity estimation information and the plant attribute information. At this time, a temporary value is set as β. As a temporary value of β, more than 0 and 10 or less can be mentioned as an example, and 1 may be used.
Due to the use of a hypothetical value for β, the ΔP _sim calculated by the method described above is a function of γ.
The value of γ can be set so that the relationship between the measured value ΔP of the pressure loss at the reaction elapsed time _tx and the ΔP _sim is ΔP=ΔP _sim .

Using β and γ obtained in this way, the estimated pressure loss ΔP _sim in the reactor at another arbitrary reaction elapsed time t _{x +1 after the reaction elapsed time t x} is calculated as porosity estimation information, plant Based on the attribute information, it is calculated from the formula (1-1), the pressure loss calculation function, and the formula (10).

When ΔP/ΔP _sim , which is the ratio of the measured pressure loss value ΔP at the reaction time t _x+1 to the ΔP _sim , is outside the range of 0.5 to 1.5, the temporary value of β is changed. , the value of γ is set again by the method described above (so that the relationship between the measured value ΔP of the pressure loss at the reaction elapsed time _tx and the ΔP _sim is ΔP=ΔP _sim ).
On the other hand, when ΔP/ΔP _sim is within the range of 0.5 to 1.5, the β and γ are used, and the reaction at another arbitrary reaction time t x ₊₂ after the reaction time t _x+1 Estimated pressure loss ΔP _sim in the vessel is calculated in the same manner as above.
When ΔP/ΔP _sim , which is the ratio of the measured pressure loss value ΔP at the reaction elapsed time t _x+2 to the ΔP _sim , is outside the range of 0.5 to 1.5, the provisional value of β as described above and set the value of γ again as described above.
On the other hand, when ΔP/ΔP _sim is within the range of 0.5 to 1.5, the β and γ are used, and the reaction at another arbitrary reaction time t _x+3 after the reaction time t _x+2 An estimated pressure loss value ΔP _sim in the vessel is calculated in the same manner as described above, and the above operation is repeated.

When the above operation is repeated and ΔP/ΔP _sim is within the range of 0.5 to 1.5 at all 15 points after the reaction time _tx , β and γ can be determined.

≪Response to application of information provision method≫
The information providing method of the present invention can be applied to reactions in which impurities in the fluid accumulate on the solid catalyst layer, thereby reducing the porosity of the solid catalyst layer. In addition, it can be applied to a reaction in which coke is generated during the reaction and deposited on the solid catalyst layer, thereby reducing the porosity of the solid catalyst layer. Such reactions include, but are not limited to, hydrotreating reactions for heavy hydrocarbon oils and hydrotreating reactions for light hydrocarbon oils. An application example of the information provision method of the present invention to the hydrotreating reaction of heavy hydrocarbon oil will be described in detail below.

<Hydrotreatment reaction of heavy hydrocarbon oil>
The hydrotreating reaction of heavy hydrocarbon oil is a two-phase fixed-bed flow system in which liquid heavy hydrocarbon oil and gaseous hydrogen are allowed to flow through a reactor. reaction. Heavy hydrocarbon oil contains metal impurities, and these metal impurities deposit on the solid catalyst layer, resulting in an increase in pressure loss over time. Metal elements contained in the metal impurities contained in the heavy hydrocarbon oil include Ni, V, Fe, Na, Zn, Al, Ba, Ca, Mg, P, Pb, Mo, Cr, Cd, As, Se, Si etc. are mentioned as a typical example. In addition, in the hydrotreating reaction of heavy hydrocarbon oil, it is necessary to raise the reaction temperature over time as the activity of the solid catalyst decreases. It is known that coke begins to deposit on solid catalyst layers and plugs the porosity of fixed catalyst layers.

First, the porosity estimation information of the user plant and the plant attribute information are received via the network, and based on the porosity estimation information, solid catalyst layer porosity calculation function 1 or solid catalyst layer porosity calculation function 2 Calculate the porosity of the solid catalyst layer.
Heavy carbonization that has flowed into the reactor during a certain period (t _x -t _x-1 ) from another arbitrary reaction elapsed time t _x-1 prior to the arbitrary reaction elapsed time t _x to the reaction elapsed time t _x The total amount of metal impurities S _IN in the hydrogen oil and the total amount of metal impurities S _OUT in the heavy hydrocarbon oil discharged from the reactor are received from the user terminal as porosity estimation information.

Acquisition of S _IN and S _OUT at the user plant can be done as follows.
S _IN is the amount of metal impurities in the heavy hydrocarbon oil immediately before flowing into the reactor during a certain period (t _x -t x- ₁ ) from the reaction time t x _-1 to the reaction time t _x It can be obtained by measuring the concentration (in units of ppm, for example) and calculating the product with the amount of heavy hydrocarbon oil (in units of, for example, kg) flowing into the reactor during that time. In addition, the S _OUT is the heavy hydrocarbon oil immediately after flowing out from the reactor during a certain period (t _x -t x _-1 ) from the reaction lapse time t _x-1 to the reaction lapse time t _x can be obtained by measuring the concentration of metal impurities (unit: ppm, for example) and calculating the product with the amount (unit: kg, for example) of heavy hydrocarbon oil discharged from the reactor during that time. In the present embodiment, S _IN and S _OUT may be metal compound equivalent amounts or metal equivalent amounts, but are preferably metal equivalent amounts.

ICP-MS, for example, can be used as a method for measuring the concentration of metal impurities in a user plant. The amount of heavy hydrocarbon oil that has flowed into the reactor and the amount of heavy hydrocarbon oil that has flowed out of the reactor can be obtained, for example, by flow meters.

In addition, since the hydrogen used for the hydrotreating reaction of heavy hydrocarbon oil usually does not contain impurities deposited on the solid catalyst layer, in calculating the S _IN and the S _OUT , It is not necessary to measure the impurity concentration of

By substituting the received S _IN and S _OUT into the above equation (1), the porosity ε _x of the solid catalyst layer in the reactor at the reaction time t _x can be obtained. The porosity ε ₀ of the solid catalyst layer in the reactor at the start of the reaction can be obtained by the method described above, and ε _x−1 is obtained by repeatedly applying the above formula (1) from ε ₀ . be able to.

In the present embodiment, the reaction temperature Tt _(x) at the reaction elapsed time _tx is further received from the user terminal as the porosity estimation information, and the relationship between the Tt _(x) and the coking threshold T _B is T When _t(x) >T _B is satisfied, in the porosity calculation step, instead of the formula (1), the formula (1-1) is replaced with the S _IN , the S _OUT , the T _B , and the T _t It is preferable to obtain the porosity ε _x of the solid catalyst layer in the reactor at the reaction elapsed time t _x by substituting _(x) .

Based on the porosity of the solid catalyst layer obtained as described above and the plant attribute information received from the user terminal, the pressure loss estimation value in the reactor of the user plant is calculated by the pressure loss estimation calculation function.
The plant attribute information in the present embodiment preferably includes information on properties of the fluid, information on the filling configuration of the solid catalyst, and information on the type of the solid catalyst.

Information about the properties of the fluid in this embodiment includes the viscosity μ _L , density ρ _L , and linear velocity u L of heavy hydrocarbon oil, and the viscosity μ _G , density _{ρ G ,} and linear velocity u _G of hydrogen.

The viscosity μ _L [kg/ms] of the heavy hydrocarbon oil at the reaction temperature of the user plant is, for example, the result obtained from JIS K 2283 “Crude oil and petroleum products-Kinematic viscosity test method and viscosity index calculation method” and JIS K2249 It can be obtained by multiplying the 15° C. converted density obtained by “Crude Oil and Petroleum Products—Density Test Method and Density/Mass/Volume Conversion Table” and converting to temperature.
The density ρ _L [kg/m ³ ] of the heavy hydrocarbon oil at the reaction temperature of the user plant is, for example, 15° C. obtained according to JIS K2249 “Crude oil and petroleum products—Density test method and density/mass/capacity conversion table”. It can be obtained by correcting the converted density with temperature.
The linear velocity u _L [m/s] of the heavy hydrocarbon oil in ^the user plant is the cross-sectional area of the reactor (for example, a cylindrical tubular reactor) It can be obtained by dividing by [m ² ]. The flow rate of heavy hydrocarbon oil can be obtained, for example, by a flow meter.

The viscosity μ _G [kg/ms] of hydrogen at the reaction temperature of the user plant can be obtained by introducing the compositional analysis results obtained by, for example, gas chromatography into a process simulator and calculating the results.
The density ρ _G [kg/m ³ ] of hydrogen at the reaction temperature of the user plant can be obtained, for example, by correcting the density corresponding to the composition of the composition analysis result obtained by gas chromatography with the temperature.
The linear velocity u _G [m/s] of hydrogen in the user plant is obtained by dividing the flow rate [m ³ /s] of hydrogen by the cross-sectional area [m ² ] of the reactor (for example, a cylindrical tubular reactor). can be obtained by The hydrogen flow rate can be obtained, for example, with a gas meter.

Information related to the packing structure of the solid catalyst in this embodiment includes the layer height H [m] of the solid catalyst layer, and the acquisition method in the user plant is as described above.

Information related to the type of solid catalyst in this embodiment includes the sphere diameter dp [m] when the solid catalyst is assumed to be a sphere, and the acquisition method in the user plant is as described above.

When the Ergun-Larkins formula is used as the pressure loss calculation function, ε _x , μ _L , ρ _L , and u _L calculated by the above formula (1) or the above formula (1-1) are converted into the above formula (8). Substitute to calculate _δL . Also, ε _x , μ _G , ρ _G , and u _G calculated by the above equation (1) or the above equation (1-1) are substituted into the above equation (9) to calculate δ _G.

χ=( _δL / _δG ) ^1/2 is calculated from the obtained _δL and _δG . Subsequently, using δ _L , δ _G , and χ, δ _LG is calculated from the above equation (4), and R _L is calculated from the above equation (5). Subsequently, using the obtained _RL , _ρm is calculated from the above equation (6). Then, using the obtained δ _LG and ρ _m , the calculated pressure loss value ΔP2 _cal is calculated from the above equation (7). Then, by substituting the obtained ΔP2 _cal into the ΔP _cal of the formula (10), which is the correction function for each reactor, the reaction at the reaction elapsed time t _x in the method for hydrotreating heavy hydrocarbon oil An in-vessel pressure drop estimate ΔP _sim (ΔP2 _sim ) can be determined.

≪How to use the information provision method≫
As a method of using the information indicating the estimated value of pressure loss in the reactor of the user plant of the present invention provided by the information providing method of the present invention, for example, (1) Confirmation of an abnormal increase in pressure loss during reaction operation, (2) Estimation of when the reaction should be terminated, (3) Estimation of pressure loss transition until the end of the operation period for the operation plan, (4) Estimation of operating conditions under which the pressure loss is less than the allowable pressure loss for the operation period etc. are mentioned as an example.

(Confirmation of abnormal increase in pressure loss during reaction operation)
Using the porosity ε _x of the solid catalyst layer calculated by the above formula (1) of the present invention, when the pressure loss estimated value ΔP _sim obtained by the pressure loss estimation method and the measured value ΔP are significantly different (especially ΔP/ΔP _sim >1.5), it is suggested that the increase in pressure loss is caused not only by deposition of impurities in the fluid on the solid catalyst layer but also by other factors. be. For example, coke is generated, and the coke begins to deposit on the solid catalyst layer, which gradually closes the pores of the solid catalyst layer, thereby increasing the pressure loss. In this case, by resetting the tuning parameter α, the change over time of the pressure loss can be estimated again. The method of resetting the tuning parameter α is as described above. Alternatively, the porosity ε _x of the solid catalyst layer calculated by the above formula (1-1) may be used to obtain the pressure loss estimated value ΔP _sim by the method described above. The method using the formula (1-1) does not require changing the tuning parameter α, and is therefore preferable to the method of resetting the tuning parameter α described above.

(Estimation of when the reaction should be terminated)
By plotting the estimated pressure drop obtained by the information providing method of the present invention against the reaction time and creating a pressure drop estimation curve connecting these plots, the allowable pressure drop set for the reactor It is possible to estimate the reaction time to reach , and to determine when to terminate the reaction with reference to this time. In addition, by substituting predicted values such as future operating conditions and amount of deposition of impurities into the above formula, the allowable value set for the reactor can be obtained by plotting the future pressure loss estimated value against the reaction time. The reaction time to reach the pressure loss can be estimated, and the time to terminate the reaction can be determined with reference to this time.

(Estimation of changes in pressure loss until the end of the operation period for the operation plan)
From the estimated pressure loss obtained from the information provision method of the present invention and the future operating conditions, the pressure loss until the end of the operation period can be estimated, and it can be confirmed that the pressure loss will be less than the allowable pressure loss under these operating conditions.

(Estimation of operating conditions under which the pressure loss is less than the allowable pressure loss for the operating period)
It is possible to estimate the pressure loss estimated value obtained from the information provision method of the present invention, the type of raw material and the operating conditions that will cause the pressure loss to be equal to or less than the allowable pressure loss until the end of the operating period.
Specifically, a desired pressure loss estimation value is input to the pressure loss estimation calculation function, and the porosity estimation information and the plant for the solid catalyst layer porosity calculation function and the pressure loss estimation calculation function to hold A combination of attribute information can be estimated. By changing the reaction conditions based on the estimated porosity estimation information and plant attribute information, the desired pressure loss can be achieved. An example of changing the reaction conditions based on the porosity estimation information is to change to a fluid with a different amount of impurities. Changing the reaction conditions based on the plant attribute information includes changing to fluids with different densities and viscosities, and changing the linear velocity of the fluids. Among these, it is preferable to change the reaction conditions based on the plant attribute information, and it is more preferable to change the linear velocity of the fluid.

≪Pressure loss estimation calculation device≫
Another embodiment of the present invention comprises a processor and storage means for storing computer readable instructions, wherein when said computer readable instructions are executed by said processor, from a user terminal, a user having a solid catalyst layer formed thereon. Receiving porosity estimation information and plant attribute information via a network with respect to a fixed bed flow reaction in which a one-phase gas or liquid fluid or a two-phase gas and liquid fluid is circulated in a plant reactor. Then, based on the received porosity estimation information, the solid catalyst layer porosity calculation function is used to calculate the porosity of the solid catalyst layer in the reactor of the user plant, and based on the porosity and the plant attribute information , a pressure loss estimation calculation device (hereinafter referred to as , also simply referred to as an “estimation device”).

An information providing system 100 including the estimation device of this embodiment will be described. FIG. 2 is a diagram showing a system configuration example of the information providing system 100. As shown in FIG. The information providing system 100 includes one or more control devices 30 , a monitoring control device 40 , an estimation device 50 and a terminal device 60 . The monitor control device 40 and the terminal device 60 are specific examples of user terminals.
The control device 30 and the monitoring control device 40 are communicably connected. The monitoring control device 40, the estimation device 50, and the terminal device 60 are connected via a network 70 so as to be communicable. The network 70 may be configured by a wireless communication network, may be configured by a wired communication network, or may be configured by combining a wireless communication network and a wired communication network. The network 70 may be a wide area communication network, a local communication network, or a single cable. In other words, the network 70 may be configured in any way as long as it is a communication channel capable of transmitting data.

The control device 30 is configured using an information processing device such as a Programmable Logic Controller (PLC), a single board computer, or a personal computer. The control device 30 provides state values (voltage value, rotation speed, etc.) indicating the state of the equipment to be controlled, physical quantities related to the object to be monitored (the above-described porosity estimation information and plant attribute information, actual pressure loss values, etc.) to get values such as The control device 30 transmits each acquired value to the monitoring control device 40 .
The details of the porosity estimation information and the plant attribute information are as described above.

In addition, the control device 30 controls the operation of devices such as actuators connected in advance to the control device 30 . The control device 30 controls the operation of the equipment according to predefined conditions, for example, based on the estimation result (pressure loss estimated value) by the estimation device 50, the acquired state value, the physical quantity, and the like. For example, if the pressure drop estimate exceeds a predetermined threshold, controller 30 may be configured to deactivate a particular piece of equipment.

The monitor control device 40 is configured using an information processing device such as a personal computer, a server device, or a dedicated device. When the monitoring control device 40 acquires the state values and physical quantities from each control device 30, the monitoring and control device 40 records the acquired state values and physical quantities in the storage device in association with date and time information. The monitoring control device 40 transmits predetermined values among the obtained state values and physical quantities to the estimation device 50 via the network 70 . The transmitted values include, for example, the elapsed reaction time, the above-described porosity estimation information and plant attribute information, and the measured value of pressure loss. The supervisory control device 40 receives information from the estimation device 50 via the network 70 . Information received includes, for example, pressure drop estimates. The monitoring control device 40 transmits the received information to the control device 30 .

The supervisory control device 40 may comprise an input device and an output device. The input device is configured using existing input devices such as a keyboard, pointing device (mouse, tablet, etc.), buttons, and touch panel. The input device may be configured using a microphone and voice recognition device. In this case, the input device recognizes the words uttered by the user, and inputs the character string information of the recognition result to the monitor control device 40 . The input device may be configured in any way as long as it can input a user's instruction to the monitor control device 40 . The output device may be configured using, for example, a device that outputs images and characters to a screen. For example, the output device can be configured using a CRT (Cathode Ray Tube), a liquid crystal display, an organic EL (Electro-Luminescent) display, or the like. Also, the output device may be configured using a device that prints (prints) images and characters on a sheet. For example, the output device can be configured using an inkjet printer, a laser printer, or the like. Also, the output device may be configured using a device that converts characters into voice and outputs the voice. In this case, the output device can be configured using a speech synthesizer and a speech output device (speaker). The output device may be configured using a light emitting device such as an LED (Light Emitting Diode). In this case, the output device may cause the light emitting device to emit light in a manner associated in advance with the information to be output, or may emit light from the light emitting device at a position associated in advance with the information to be output. good too.

The monitoring control device 40 acquires values obtained by the user operating the input device. For example, the output device outputs each value input via the input device, each value obtained from each control device 30, the value of the estimation result by the estimation device 50, and the like. For example, when the value of the estimation result satisfies a predetermined condition (for example, a condition such as exceeding a threshold value), the monitor control device 40 may cause the output device to output information indicating that fact.

The estimating device 50 receives the porosity estimation information and the plant attribute information via the network, and uses the solid catalyst layer porosity calculation function 1 based on the received porosity estimation information to determine the inside of the reactor of the user plant. Calculate the porosity of the solid catalyst layer, calculate the pressure loss estimated value in the reactor of the user plant by the pressure loss estimation calculation function based on the porosity and the plant attribute information, and calculate the calculated Sending information indicative of the pressure drop estimate to the user terminal.
The details of the solid catalyst layer porosity calculation function 1 and the pressure loss estimation calculation function are as described above.

At the initial stage of the reaction, the estimating device 50 calculates tuning parameters based on the measured value of the pressure loss in the reactor received via the network, the porosity estimation information, and the plant attribute information. When using the above formula (1) as the solid catalyst layer porosity calculation function 1 and using the above formula (10) as the correction function for each reactor in the pressure loss estimation calculation function, the tuning parameter α in the above formula (1) , and the tuning parameter σ of the above equation (10) is calculated. Then, using the calculated parameters, the pressure loss estimated value is calculated by the method described above.

When the porosity estimation information includes information indicating the reaction temperature Tt _(x) of the solid catalyst layer, the estimation device 50 compares Tt _(x) with a preset coking threshold T _B , T _t(x) >T _B , instead of the solid catalyst layer porosity calculation function 1, the solid catalyst layer porosity calculation function 2 is used to calculate the porosity of the solid catalyst layer in the reactor of the user plant. can be calculated. The details of the solid catalyst layer porosity calculation function 2 are as described above.

In the early stage after the relationship between T _t(x) and T _B satisfies T _t(x) >T _B , the estimating device 50 receives the measured value of the pressure loss in the reactor via the network and the air gap Tuning parameters are calculated based on the rate estimation information and the plant attribute information. When using the formula (1-1) as the solid catalyst layer porosity calculation function 2, the tuning parameters β and γ of the formula (1-1) are calculated. Then, using the calculated parameters, the pressure loss estimated value is calculated by the method described above.

The estimation device 50 is configured using an information processing device such as a personal computer, a server device, or a dedicated device. The estimation device 50 may be configured using one or a plurality of information processing devices. For example, the estimating device 50 may be constructed as a cluster machine, may be constructed as a cloud, or may be constructed in any manner. The estimation device 50 includes a communication section 51 and a calculation section 15 . Note that the calculation unit 15 included in the estimating device 50 is a specific example of a configuration for acquiring the pressure loss estimated value, and the estimating device 50 may be provided with other configurations. That is, the estimation device 50 receives the porosity estimation information and the plant attribute information via the network, and uses the solid catalyst layer porosity calculation function 1 or 2 based on the received porosity estimation information. calculating the porosity of the solid catalyst layer in the reactor, and calculating an estimated pressure loss value in the reactor of the user plant by a pressure loss estimation calculation function based on the porosity and the plant attribute information; Any device may be used as long as it can transmit information indicating the calculated pressure loss estimated value to the user terminal. The communication unit 51 is configured using a network interface. The communication unit 51 receives data transmitted from the monitoring control device 40 via the network 70 . Communication unit 51 outputs the received value to calculation unit 15 . Further, the communication unit 51 transmits the calculation result (for example, pressure loss estimated value) of the calculation unit 15 to a predetermined device. The predetermined device is the monitoring control device 40, for example. The calculation unit 15 is a device equivalent to the calculation unit 15 described above.

The terminal device 60 is a communicable information processing device such as a personal computer, a smart phone, or a tablet. When the state value and the physical quantity are input by the user, the terminal device 60 transmits the input state value and physical quantity to the estimation device 50 via the network 70 . Upon receiving the value of the estimation result from the estimation device 50, the terminal device 60 outputs the received value. For example, when the value of the estimation result satisfies a predetermined condition (for example, a condition such as exceeding a threshold value), the terminal device 60 may display or audibly output information indicating that fact.

The reaction to the application of the information providing system of this embodiment includes the same reaction as the reaction to the application of the information providing method described above.

Further, in the present embodiment, a pressure loss estimation program for causing a computer to function as a pressure loss estimation calculation device and a computer non-temporary readable recording medium storing the program are provided. Examples of non-temporarily readable recording media for computers include magnetic tapes (digital data storage (DSS), etc.), magnetic disks (hard disk drives (HDD), flexible disks (FD), etc.), optical disks (compact discs (CD), digital versatile disc (DVD), Blu-ray disc (BD), etc.), magneto-optical disc (MO), flash memory (SSD (Solid State Drive), memory card, USB memory, etc.).

DESCRIPTION OF SYMBOLS 15... Calculation part, 30... Control apparatus, 40... Monitoring control apparatus, 50... Estimation apparatus, 51... Communication part, 60... Terminal device, 70... Network, 100... Information provision system 100

Claims (12)

Regarding a fixed bed flow reaction in which an information processing device circulates a one-phase gas or liquid fluid or a two-phase gas and liquid fluid from a user terminal to a reactor of a user plant in which a solid catalyst layer is formed, receiving porosity estimation information and plant attribute information via a network;
a porosity calculation step in which the information processing device calculates the porosity of the solid catalyst layer in the reactor of the user plant using the solid catalyst layer porosity calculation function 1 based on the received porosity estimation information;
A pressure loss in which an information processing device calculates an estimated value of pressure loss in the reactor at an arbitrary reaction elapsed time t _x of the user plant using a pressure loss estimation calculation function based on the porosity and the plant attribute information. a calculation step;
An information providing method comprising the step of transmitting information indicating the calculated pressure loss estimated value in the reactor at an arbitrary reaction elapsed time _tx of the user plant to the user terminal, wherein
the fluid contains impurities that can deposit on the solid catalyst layer;
The porosity estimation information is supplied to the reactor during (t x -t x-1 ) _{from another} arbitrary reaction elapsed time t _x-1 prior _to the reaction elapsed time t _x to the reaction elapsed time t x including a total impurity amount S _IN in the inflow fluid and a total impurity amount S _OUT in the fluid outflow from the reactor ;
The solid catalyst layer porosity calculation function 1 is represented by the following formula (1),
The pressure loss estimation calculation function is composed of a pressure loss calculation function and a correction function for each reactor,
The pressure loss calculation function is Ergun's formula, Blake-Kozeny's formula, Burke-Plummer's formula, Kozeny-Carman's formula, or Fanning's formula when the fluid is one phase of gas or liquid, and the fluid is gas and liquid. In the case of two phases, the Ergun-Larkins or Lockhart-Martinelli equation,
The correction function for each reactor is represented by the following formula (10),
The porosity calculating step substitutes the received S _IN and S _OUT into the formula (1) to calculate the porosity of the solid catalyst layer in the reactor of the user plant at the reaction elapsed time _tx . is a porosity calculation step for
The pressure loss calculation step is a step of substituting the porosity and the received plant attribute information into the pressure loss calculation function to calculate a pressure loss calculation value in the reactor of the user plant at the reaction elapsed time tx _. and a step of calculating an estimated pressure loss value in the reactor of the user plant at the reaction elapsed time _tx by substituting the calculated pressure loss value into the equation (10). can be,
The tuning parameters α and σ in the formulas (1) and (10) are determined by the information processing device at the initial stage of the reaction based on the measured value of the pressure loss in the reactor, the porosity estimation information, and the plant attribute information. An information providing method, which is a calculated tuning parameter.

(In the above formula (1), ε _x is the porosity of the solid catalyst layer in the reactor at the reaction time t _x , and ε _x-1 is the solid catalyst layer in the reactor at the reaction time t _x-1. S _IN is the total amount of impurities in the fluid that flowed into the reactor during a certain period from the time t _x−1 of the reaction to the time t _x , and S _OUT is the total amount of impurities from the time t _x−1 of the reaction. is the total amount of impurities in the fluid flowing out of the reactor for a certain period of time up to the reaction elapsed time tx _, and α is a constant tuning parameter)

(In equation (10) above, ΔP _sim is the pressure drop estimate, ΔP _cal is the pressure drop calculation, and σ is a constant tuning parameter.) 2. The plant attribute information according to claim 1, wherein the plant attribute information includes at least one type of information selected from the group consisting of information on the properties of the fluid, information on the filling configuration of the solid catalyst, and information on the type of the solid catalyst. Method. The fluid contains a component that can generate coke, the porosity estimation information includes information indicating the reaction temperature Tt _(x) of the solid catalyst layer, the Tt _(x) and coke are generated, When the relation of the coking threshold T _B , which is the temperature at which the coke starts to deposit on the solid catalyst layer, satisfies T _t(x) >T _B , in the porosity calculation step, the solid catalyst layer porosity calculation function 1 Instead of calculating the porosity of the solid catalyst layer in the reactor of the user plant by the solid catalyst layer porosity calculation function 2,
The solid catalyst layer porosity calculation function 2 is represented by the following formula (1-1),
The porosity calculation step substitutes the received T _t(x) , S _IN , and S _OUT into the equation ( _1-1 ) to 3. The method according to claim 1 or 2 , which is a porosity calculation step of calculating the porosity of the solid catalyst layer inside .

(In the above formula (1-1), T _{t (x)} is the reaction temperature of the solid catalyst layer at the reaction elapsed time t _x , T _B is the coking threshold value, R is the gas constant, and β and γ are constants. Tuning parameters, ε _x , ε _x−1 , α, S _IN , and S _OUT are the same as in the above formula (1).) The solid catalyst layer porosity calculation function 2 is used by the information processing device in the initial stage after the relationship between the T _t(x) and the T _B satisfies T _t(x) >T _B , 4. The method according to claim 3 , wherein tuning parameters calculated based on the measured value of pressure loss and the porosity estimation information and the plant attribute information are used. The method according to any one of claims 1 to 4 , wherein the fixed bed flow reaction is a hydrotreating reaction for heavy hydrocarbon oils or a hydrotreating reaction for light hydrocarbon oils. Porosity estimation information and porosity estimation information for a fixed bed flow reaction in which a one-phase fluid of gas or liquid, or a two-phase fluid of gas and liquid is circulated from a user terminal to a reactor of a user plant in which a solid catalyst layer is formed. , and plant attribute information via a network ;
calculating the porosity of the solid catalyst layer in the reactor of the user plant by the solid catalyst layer porosity calculation function 1 based on the received porosity estimation information;
a calculation unit that calculates an estimated pressure loss value in the reactor at an arbitrary reaction elapsed time tx _of the user plant by a pressure loss estimation calculation function based on the porosity and the plant attribute information,
The communication unit is a pressure loss estimation calculation device that transmits information indicating the calculated pressure loss estimated value in the reactor at an arbitrary reaction elapsed time tx of _the user plant to the user terminal ,
the fluid contains impurities that can deposit on the solid catalyst layer;
The porosity estimation information is supplied to the reactor during (t x -t x-1 ) _{from another} arbitrary reaction elapsed time t _x-1 prior _to the reaction elapsed time t _x to the reaction elapsed time t x including a total impurity amount S _IN in the inflow fluid and a total impurity amount S _OUT in the fluid outflow from the reactor ;
The solid catalyst layer porosity calculation function 1 is represented by the following formula (1),
The pressure loss estimation calculation function is composed of a pressure loss calculation function and a correction function for each reactor,
The pressure loss calculation function is Ergun's formula, Blake-Kozeny's formula, Burke-Plummer's formula, Kozeny-Carman's formula, or Fanning's formula when the fluid is one phase of gas or liquid, and the fluid is gas and liquid. In the case of two phases, the Ergun-Larkins or Lockhart-Martinelli equation,
The correction function for each reactor is represented by the following formula (10),
Calculation of the porosity of the solid catalyst layer in the reactor of the user plant is performed by substituting the received S _IN and S _OUT into the formula (1),
Calculation of the estimated pressure loss value in the reactor of the user plant is performed by substituting the porosity and the received plant attribute information into the pressure loss calculation function _, By calculating the calculated pressure loss value of the solid catalyst layer in the inside and substituting the calculated pressure loss value into the formula (10),
The tuning parameters α and σ in the formulas (1) and (10) are determined by the information processing device at the initial stage of the reaction based on the measured value of the pressure loss in the reactor, the porosity estimation information, and the plant attribute information. A pressure loss estimation calculator, which is the calculated tuning parameter .

(In the above formula (1), ε _x is the porosity of the solid catalyst layer in the reactor at the reaction time t _x , and ε _x-1 is the solid catalyst layer in the reactor at the reaction time t _x-1. S _IN is the total amount of impurities in the fluid that flowed into the reactor during a certain period from the time t _x−1 of the reaction to the time t _x , and S _OUT is the total amount of impurities from the time t _x−1 of the reaction. is the total amount of impurities in the fluid flowing out of the reactor for a certain period of time up to the reaction elapsed time tx _, and α is a constant tuning parameter)

(In equation (10) above, ΔP _sim is the pressure drop estimate, ΔP _cal is the pressure drop calculation, and σ is a constant tuning parameter.) 7. The plant attribute information according to claim 6 , wherein said plant attribute information includes at least one type of information selected from the group consisting of information on properties of said fluid, information on filling configuration of said solid catalyst, and information on type of said solid catalyst. Pressure loss estimation calculator. The fluid contains a component that can generate coke, the porosity estimation information includes information indicating the reaction temperature Tt _(x) of the solid catalyst layer, the Tt _(x) and coke are generated, When the relationship of the coking threshold T _B , which is the temperature at which the coke starts to deposit on the solid catalyst layer , satisfies T _t(x) >T _B , in the calculation of the porosity, the solid catalyst layer porosity calculation function 1 Instead of calculating the porosity of the solid catalyst layer in the reactor of the user plant by the solid catalyst layer porosity calculation function 2,
The solid catalyst layer porosity calculation function 2 is represented by the following formula (1-1),
Calculation of the porosity of the solid catalyst layer in the reactor of the user plant is performed by substituting the received T _t(x) , the S _IN , and the S _OUT into the formula (1-1), The pressure loss estimation calculation device according to claim 6 or 7 .

(In the above formula (1-1), T _{t (x)} is the reaction temperature of the solid catalyst layer at the reaction elapsed time t _x , T _B is the coking threshold value, R is the gas constant, and β and γ are constants. Tuning parameters, ε _x , ε _x−1 , α, S _IN , and S _OUT are the same as in the above formula (1).) The solid catalyst layer porosity calculation function 2 is the measured value of the pressure loss in the reactor at the initial stage after the relationship between the T _t(x) and the T _B satisfies T _t(x) >T _B and a tuning parameter calculated based on the porosity estimation information and the plant attribute information. The pressure loss estimation calculation device according to any one of claims 6 to 9 , wherein the fixed bed flow reaction is a hydrotreating reaction of heavy hydrocarbon oil or a hydrotreating reaction of light hydrocarbon oil. A pressure loss estimation program for causing a computer to function as the pressure loss estimation calculation device according to any one of claims 6 to 10 . A computer non-transitory readable recording medium storing the program according to claim 11 .

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