Method, device and equipment for calculating reaction heat of storage device and hydrocracking device

Abstract

The present invention discloses a storage device, a method, a device and an equipment for calculating the reaction heat of a hydrocracking device, wherein the method comprises the following steps: collecting and analyzing data of the hydrocracking device under different working conditions respectively; respectively bringing the sulfur content, nitrogen content, oxygen content, reaction conversion rate and reference reaction heat data of multiple feedstock oils and generated oils obtained through the data collection and analysis of the hydrocracking device into a preset mathematical correlation formula to solve the preset coefficients of the mathematical correlation formula; constructing a calculation model suitable for the hydrocracking device according to the solution results of the preset coefficients; when the present invention measures the reaction heat of a certain hydrocracking device in real time, there is no need to empirically estimate the number of different types of reactions occurring in the hydrocracking process and the values ​​of various types of reaction heat, so the accuracy of the reaction heat result value can be effectively improved.

Description

Technical Field

[0001] The invention relates to the field of oil refining, and in particular to a method, device and equipment for calculating reaction heat of a storage device and a hydrocracking device. Background Art

[0002] The reaction heat of the hydrocracking process is of high quality and large volume, and the reaction heat is related to the properties of the raw materials, product quality, etc. Therefore, conducting research on the prediction and optimal utilization of the hydrocracking reaction heat is of great significance to optimizing the operation of the device and reducing the energy consumption of the device.

[0003] At present, the methods for calculating the reaction heat of the hydrocracking unit mainly include: 1. Based on the experience of technicians, the heat is obtained by adding various reaction heats such as hydrodenitrogenation reaction, hydrodesulfurization reaction, olefin hydrogenation reaction, aromatic saturation reaction, cycloalkane cracking reaction, and paraffin cracking. 2. In the laboratory, a small-scale experimental device or a medium-sized experimental device is used to simulate the high-temperature and high-pressure production process of hydrocracking to directly measure the reaction heat of the hydrocracking process.

[0004] After research, the inventors found that in the above two methods in the prior art, either the various reaction heat values ​​are estimated by experience, and the number of different types of reactions in the hydrocracking process is also estimated by experience, resulting in a large deviation from the actual production of the device; or the data such as the specific heat capacity and thermal enthalpy of raw materials and products under simulation conditions have certain errors, and the heat loss of the test equipment is difficult to measure, resulting in poor accuracy of the calculated results; therefore, the technical solutions for the reaction heat measurement of the hydrocracking unit in the prior art generally have the defect that the calculation results are poorly accurate and cannot be used to guide the operation optimization of the hydrocracking unit.

[0005] The information disclosed in this background technology section is only intended to enhance the understanding of the overall background of the invention and should not be regarded as an acknowledgment or any form of suggestion that the information constitutes the prior art already known to a person skilled in the art. Summary of the invention

[0006] The purpose of the present invention is to improve the accuracy of reaction heat calculation of a hydrocracking unit.

[0007] The present invention provides a method for calculating the reaction heat of a hydrocracking unit, comprising the steps of:

[0008] S11, respectively collecting and analyzing data on the hydrocracking unit under different working conditions, wherein the content of each data collection and analysis includes: obtaining the test analysis data of the raw materials and products of the hydrocracking unit; calculating the reaction conversion rate of the hydrocracking unit; calculating the reference reaction heat of the hydrocracking unit;

[0009] S12, respectively bringing the sulfur content, nitrogen content, oxygen content, reaction conversion rate and reference reaction heat data of the feed oil and the produced oil obtained by data collection and analysis of the hydrocracking unit into a preset mathematical correlation formula, and solving the preset coefficients of the mathematical correlation formula; the mathematical correlation formula includes:

[0010] Q 反 =a*(S in -S out ) / M oil，feed +b*(N in -N out ) / M oil，feed +c*(O in -O out ) / M oil，feed +d*K+e

[0011] Among them, Q 反 is the reference reaction heat per unit mass of crude oil; M oil，feed is the crude oil flow rate; S in S is the sulfur content of the raw oil at the reactor inlet; out is the sulfur content of the reaction effluent at the reactor outlet; N in N is the nitrogen content of the raw oil at the reactor inlet; out is the nitrogen content of the reaction effluent at the reactor outlet; in is the oxygen content of the raw oil at the reactor inlet; O out is the oxygen content of the reaction effluent at the reactor outlet; K is the conversion rate of the hydrocracking reaction; the preset coefficients include: a is the heat coefficient of the hydrodesulfurization reaction; b is the heat coefficient of the hydrodenitrogenation reaction; c is the heat coefficient of the hydrodeoxygenation reaction; d is the heat coefficient of the hydrocracking reaction; e is the heat-related constant of the hydrocracking reaction;

[0012] S13. According to the solution results of the preset coefficients, a calculation model suitable for the hydrocracking unit is constructed, wherein the calculation model includes the mathematical correlation formula into which the solution results of the preset coefficients are introduced.

[0013] The present invention also includes:

[0014] S14, collecting and analyzing data on the current operating conditions of the hydrocracking unit to obtain data on the sulfur, nitrogen, and oxygen contents and reaction conversion rates of the feed oil and the produced oil;

[0015] S15. Calculate the reaction heat of the hydrocracking unit according to the calculation model.

[0016] In the present invention, the analytical data at least include distillation range, components and density; the components at least include sulfur content, nitrogen content and oxygen content.

[0017] In the present invention, the calculation to obtain the reference reaction heat of the hydrocracking unit includes:

[0018] Carrying out material balance accounting for the hydrocracking unit through the flow of raw oil, new hydrogen supplementation, and liquid and gas products;

[0019] The applicable state equation is determined based on material balance, laboratory analysis data and process operation parameters of the hydrocracking unit; and the reference reaction heat of the hydrocracking unit is obtained according to the total input heat of the reactor inlet reactant flow and the total input heat of the reactor outlet reaction effluent.

[0020] In the present invention, the applicable state equation is determined based on material balance, laboratory analysis data and process operation parameters of the hydrocracking unit, including:

[0021] Based on material balance, laboratory analysis data and process operating parameters of the hydrocracking unit, an applicable state equation is determined using AspenPlus, Aspen Hysys or Pro-II process simulation software.

[0022] In the present invention, the reference reaction heat of the hydrocracking unit is obtained according to the total input heat of the reactor inlet reactant stream and the total input heat of the reactor outlet reaction effluent, including:

[0023] According to the temperature and pressure parameters of the raw oil, circulating hydrogen, new hydrogen and cold hydrogen at the reactor inlet, the total input heat Q1 of the reactor inlet reactant flow is obtained; according to the temperature and pressure parameters of the circulating hydrogen, low-fraction gas, gas phase product and liquid phase product at the reactor outlet, the total input heat Q2 of the reactor outlet reaction effluent is obtained, and the reference reaction heat Q of the device is obtained. R =Q 2- Q1.

[0024] In the present invention, the formula for calculating the reaction conversion rate of the hydrocracking unit includes:

[0025] Reaction conversion rate = 100% * (fraction > 350°C in the feed oil - fraction > 350°C in the product oil) / fraction > 350°C in the feed oil.

[0026] In the present invention, the hydrocracking unit comprises:

[0027] Wax oil hydrocracking unit, diesel hydrocracking unit, high pressure hydrocracking unit or medium pressure hydrocracking unit.

[0028] In another aspect of the present invention, a method for optimizing energy consumption of a hydrocracking unit is also provided, comprising:

[0029] S21. Generating a mathematical correlation equation of the hydrocracking unit according to the method for calculating the reaction heat of the hydrocracking unit as described in any one of claims 1 to 8;

[0030] S22, generating an objective function for energy consumption optimization according to the mathematical correlation formula; the objective function aims to maximize the reaction heat calculation result, and the objective function includes:

[0031] maxf=a*(S in -S out ) / M oil，feed +b*(N in -N out ) / M oil，feed +c*(O in -O out ) / M oil，feed +d*K+e

[0032] Wherein, maxf is the result of reaction heat calculation; S in S is the sulfur content of the raw oil at the reactor inlet; out is the sulfur content of the reaction effluent at the reactor outlet; N in N is the nitrogen content of the raw oil at the reactor inlet; out is the nitrogen content of the reaction effluent at the reactor outlet; in is the oxygen content of the raw oil at the reactor inlet; O out is the oxygen content of the reaction effluent at the reactor outlet; K is the conversion rate of the hydrocracking reaction; the preset coefficients include: a is the heat coefficient of the hydrodesulfurization reaction; b is the heat coefficient of the hydrodenitrogenation reaction; c is the heat coefficient of the hydrodeoxygenation reaction; d is the heat coefficient of the hydrocracking reaction; e is the heat-related constant of the hydrocracking reaction;

[0033] S23, adjusting the sulfur content, nitrogen content, and oxygen content composition in the feedstock oil, and / or adjusting the processing conversion depth, and obtaining an optimization scheme for the sulfur content, nitrogen content, and oxygen content composition of the feedstock oil and the processing conversion depth according to the objective function;

[0034] The constraints of the objective function include:

[0035] 0≤S in ≤S max ; 0≤N in ≤N max ; 0≤O in ≤O max ;

[0036] Among them, S in is the sulfur content of the crude oil after mixing feeds from various sources, N in is the nitrogen content of the crude oil after mixing feeds from multiple sources, O inIt is the oxygen content of the raw oil after mixing feeds from multiple sources.

[0037] In the present invention, the constraint conditions of the objective function also include:

[0038]

[0039] Where, ΔT b is the temperature rise of the bed at the end of the hydrocracking reactor; It is the minimum temperature rise of the bed at the end of the hydrocracking reactor, which is determined according to the production requirements of the hydrocracking unit; The maximum allowable temperature rise of the bed at the end of the hydrocracking reactor is determined based on the design data of the hydrocracking reactor and / or the requirements of the on-site device generation;

[0040] In the present invention, the calculation of the temperature rise of the bed at the end of the hydrocracking reactor includes:

[0041] Obtaining the reaction conversion rate of the hydrocracking unit;

[0042] Calculating the bed temperature rise at the end of the hydrocracking reactor according to the corresponding relationship between the reaction conversion rate of the hydrocracking unit and the bed temperature rise at the end of the hydrocracking reactor;

[0043] The corresponding relationship includes: K = f(ΔT b );

[0044] Where, ΔT b is the bed temperature rise at the end of the hydrocracking reactor; K is the reaction conversion rate of the hydrocracking unit.

[0045] In another aspect of the present invention, there is also provided a device for calculating reaction heat of a hydrocracking unit, comprising:

[0046] The data acquisition and analysis unit is used to collect and analyze data of the hydrocracking unit under different working conditions. The content of each data acquisition and analysis includes: obtaining the test analysis data of the raw materials and products of the hydrocracking unit; calculating the reaction conversion rate of the hydrocracking unit; calculating the reference reaction heat of the hydrocracking unit;

[0047] The coefficient solving unit is used to respectively bring the sulfur, nitrogen, oxygen content, reaction conversion rate and reference reaction heat data of the feedstock oil and the produced oil obtained by data collection and analysis of the hydrocracking unit into a preset mathematical correlation formula to solve the preset coefficients of the mathematical correlation formula; the mathematical correlation formula includes:

[0048] Q 反 =a*(S in -S out ) / M oil，feed +b*(Nin -N out ) / M oil，feed +c*(O in O out ) / M oil，feed +d*K+e

[0049] Among them, Q 反 is the reference reaction heat per unit mass of crude oil; M oil，feed is the crude oil flow rate; S in S is the sulfur content of the raw oil at the reactor inlet; out is the sulfur content of the reaction effluent at the reactor outlet; N in N is the nitrogen content of the raw oil at the reactor inlet; out is the nitrogen content of the reaction effluent at the reactor outlet; in is the oxygen content of the raw oil at the reactor inlet; O out is the oxygen content of the reaction effluent at the reactor outlet; K is the conversion rate of the hydrocracking reaction; the preset coefficients include: a is the heat coefficient of the hydrodesulfurization reaction; b is the heat coefficient of the hydrodenitrogenation reaction; c is the heat coefficient of the hydrodeoxygenation reaction; d is the heat coefficient of the hydrocracking reaction; e is the heat-related constant of the hydrocracking reaction;

[0050] The calculation model construction unit is used to construct a calculation model suitable for the hydrocracking unit according to the solution results of the preset coefficients, and the calculation model includes the mathematical association formula that incorporates the solution results of the preset coefficients.

[0051] In another aspect of the present invention, a memory is provided, comprising a software program, wherein the software program is suitable for a processor to execute the steps of the above-mentioned method for estimating the reaction heat of a hydrocracking unit.

[0052] On the other hand, an embodiment of the present invention further provides a device for calculating the heat of reaction of a hydrocracking unit, wherein the device comprises a computer program stored in a memory, wherein the computer program comprises program instructions. When the program instructions are executed by a computer, the computer executes the methods described in the above aspects and achieves the same technical effects.

[0053] Compared with the prior art, the present invention has the following beneficial effects:

[0054] In the present invention, a mathematical correlation formula is first constructed to express the relationship between the data of the specific components such as sulfur content, nitrogen content and oxygen content in the raw oil at the reactor inlet and the reaction effluent at the reactor outlet and the reaction conversion rate and reaction heat. Then, the preset coefficients in the mathematical correlation formula are solved by performing data collection and analysis on the specific hydrocracking unit and calculating the reaction conversion rate and reaction heat, so that a calculation model suitable for the specific hydrocracking unit can be generated. The calculation model in the present invention is generated based on multiple data collection, analysis and calculation of the raw oil and each product of the specific hydrocracking unit, so that the reaction heat of the specific hydrocracking unit can be accurately calculated based on the measured specific components.

[0055] As can be seen from the above, compared with the prior art method of obtaining the reaction heat by summing up various types of reaction heat such as hydrodenitrogenation reaction, hydrodesulfurization reaction, olefin hydrogenation reaction, aromatics saturation reaction, cycloalkane cracking reaction, and paraffin cracking, the present invention does not need to empirically estimate the number of different types of reactions occurring in the hydrocracking process and the values ​​of various types of reaction heat when measuring the reaction heat of a certain hydrocracking unit in real time, thereby effectively improving the accuracy of the reaction heat result value.

[0056] In addition, compared with another prior art method of measuring the combustion heat data of the feedstock oil and products of the hydrocracking unit in the laboratory and then calculating the difference in the combustion heat of the feedstock oil and the products to obtain the reaction heat, the present invention does not need to measure the accurate combustion heat data of the feedstock oil and each product when calculating the reaction heat of the hydrocracking unit, thereby reducing the dependence on experimental analysis and reducing the complexity and difficulty of measuring the reaction heat of the hydrocracking unit in actual production.

[0057] The above description is only an overview of the technical solution of the present invention. In order to more clearly understand the technical means of the present invention and implement it according to the contents of the specification, and to make the above and other purposes, technical features and advantages of the present invention easier to understand, one or more preferred embodiments are listed below and described in detail with the accompanying drawings as follows. BRIEF DESCRIPTION OF THE DRAWINGS

[0058] Figure 1 It is a step diagram of the method for calculating the reaction heat of the hydrocracking unit described in the present invention;

[0059] Figure 2 is a step diagram of the method for optimizing energy consumption of a hydrocracking unit described in the present invention;

[0060] Figure 3 It is a schematic diagram of the structure of the reaction heat calculation device of the hydrocracking unit described in the present invention;

[0061] Figure 4 It is a schematic diagram of the structure of the reaction heat calculation equipment of the hydrocracking unit described in the present invention. DETAILED DESCRIPTION

[0062] The specific implementation modes of the present invention are described in detail below in conjunction with the accompanying drawings, but it should be understood that the protection scope of the present invention is not limited by the specific implementation modes.

[0063] Unless explicitly stated otherwise, throughout the specification and claims, the term “comprise” or variations such as “include” or “comprising”, etc., will be understood to include the stated elements or components but not to exclude other elements or components.

[0064] In this document, the terms "first", "second", etc. are used to distinguish two different elements or parts, and are not used to limit a specific position or relative relationship. In other words, in some embodiments, the terms "first", "second", etc. can also be interchangeable.

[0065] Embodiment 1

[0066] In order to improve the accuracy of reaction heat calculation of hydrocracking unit, Figure 1 As shown, in an embodiment of the present invention, a method for calculating reaction heat of a hydrocracking unit is provided, comprising the steps of:

[0067] S11, respectively collecting and analyzing data on the hydrocracking unit under different working conditions, wherein the content of each data collection and analysis includes: obtaining the test analysis data of the raw materials and products of the hydrocracking unit; calculating the reaction conversion rate of the hydrocracking unit; calculating the reference reaction heat of the hydrocracking unit;

[0068] The hydrocracking unit in the embodiment of the present invention may specifically be a wax oil hydrocracking unit, a diesel hydrocracking unit, a high pressure hydrocracking unit or a medium pressure hydrocracking unit.

[0069] In practical applications, the analytical data to be collected in the embodiments of the present invention need to include at least data such as distillation range, components and density; wherein the components need to include at least component data such as sulfur content, nitrogen content and oxygen content.

[0070] Specifically in the embodiment of the present invention, when calculating the reaction conversion rate of the hydrocracking unit, the formula used may be:

[0071] Reaction conversion rate = 100% * (fraction > 350°C in feedstock oil - fraction > 350°C in product oil) / fraction > 350°C in feedstock oil;

[0072] The steps for calculating the reference reaction heat of the hydrocracking unit in the embodiment of the present invention may specifically be:

[0073] First, the material balance of the hydrocracking unit is calculated by the feedstock oil, new hydrogen, and the flow rates of liquid and gas products;

[0074] Next, the applicable state equation is determined based on material balance, laboratory analysis data and process operating parameters of the hydrocracking unit; and the reference reaction heat of the hydrocracking unit is obtained based on the total input heat of the reactor inlet reactant flow and the total input heat of the reactor outlet reaction effluent.

[0075] In practical applications, when determining the applicable state equation, the applicable state equation can be determined based on material balance, laboratory analysis data and process operation parameters of the hydrocracking unit, using Aspen Plus, Aspen Hysys or Pro-Ⅱ process simulation software. Then, according to the temperature and pressure parameters of the reactor inlet raw oil, circulating hydrogen, new hydrogen, and cold hydrogen, the total input heat Q1 of the reactor inlet reaction flow is obtained; according to the temperature and pressure parameters of the reactor outlet circulating hydrogen, low-fraction gas, gas phase product and liquid phase product, the total input heat Q2 of the reactor outlet reaction effluent is obtained, and the reference reaction heat Q of the hydrocracking unit is obtained. R =Q 2- Q1.

[0076] S12, respectively, the sulfur, nitrogen, oxygen content, reaction conversion rate and reference reaction heat data of the feedstock oil and the produced oil obtained by data collection and analysis of the hydrocracking unit are brought into a preset mathematical correlation formula to solve the preset coefficients of the mathematical correlation formula; the mathematical correlation formula includes:

[0077] Q 反 =a*(S in -S out ) / M oil，feed +b*(N in -N out ) / M oil，feed +c*(O in -O out ) / M oil，feed +d*K+e

[0078] Among them, Q 反 is the reference reaction heat per unit mass of crude oil; S in S is the sulfur content of the raw oil at the reactor inlet; out is the sulfur content of the reaction effluent at the reactor outlet; N in N is the nitrogen content of the raw oil at the reactor inlet; out is the nitrogen content of the reaction effluent at the reactor outlet; in is the oxygen content of the raw oil at the reactor inlet; O outis the oxygen content of the reaction effluent at the reactor outlet; K is the conversion rate of the hydrocracking reaction; the preset coefficients include: a is the heat coefficient of the hydrodesulfurization reaction; b is the heat coefficient of the hydrodenitrogenation reaction; c is the heat coefficient of the hydrodeoxygenation reaction; d is the heat coefficient of the hydrocracking reaction; e is the heat-related constant of the hydrocracking reaction; M oil，feed is the crude oil flow rate.

[0079] In the embodiment of the present invention, data collection and analysis of the hydrocracking unit and calculation of the reaction conversion rate and the reference reaction heat are performed multiple times, that is, corresponding data collection and analysis and calculation of the reaction conversion rate and the reference reaction heat are required for different operating conditions.

[0080] In an embodiment of the present invention, a mathematical correlation is set to express the relationship between the data of specific components such as sulfur content, nitrogen content and oxygen content in the raw oil at the reactor inlet and the reaction effluent at the reactor outlet and the reaction conversion rate and reaction heat.

[0081] By respectively bringing the data results of each data collection and analysis (including: sulfur content of the feedstock at the reactor inlet, sulfur content of the reaction effluent at the reactor outlet, nitrogen content of the feedstock at the reactor inlet, nitrogen content of the reaction effluent at the reactor outlet, oxygen content of the feedstock at the reactor inlet, and oxygen content of the reaction effluent at the reactor outlet), as well as the corresponding calculation results of the reaction conversion rate and the reference reaction heat, into the above-mentioned mathematical correlation formula, the hydrodesulfurization reaction heat coefficient a, the hydrodenitrogenation reaction heat coefficient b, the hydrodeoxygenation reaction heat coefficient c, the hydrocracking reaction heat coefficient d, and the hydrocracking reaction heat-related constant e can be solved to obtain.

[0082] The specific steps of obtaining the mathematical correlation formula in the embodiment of the present invention may be:

[0083] S121. Collect and analyze data from the hydrocracking unit to obtain data samples. The greater the number of data samples, the more accurate the values ​​of the preset coefficients in the mathematical correlation equation will be.

[0084] In practical applications, the number of data samples in the embodiments of the present invention may be between 10 and 500. In order to balance the accuracy of the results and the amount of calculation, preferably, the number of data samples may be further between 50 and 150.

[0085] S122. Determine the content and reaction heat of specific components (specific components include sulfur content, nitrogen content or oxygen content) in the crude oil of each sample in the data sample; wherein, the content of the specific component is obtained according to the test analysis data and based on the material balance calculation, and the reaction heat is calculated as follows: based on the material balance, test analysis data, and device process operation parameters, use Aspen Plus, Aspen Hysys, Pro-Ⅱ and other process simulation software to select a suitable state equation. According to the temperature and pressure parameters of the raw oil, circulating hydrogen, new hydrogen, and cold hydrogen at the reactor inlet, the total input heat Q1 of the reaction flow at the reactor inlet is obtained; according to the temperature and pressure parameters of the circulating hydrogen, low-fraction gas, gas phase product, and liquid phase product at the reactor outlet, the total input heat Q2 of the reaction effluent at the reactor outlet is obtained, and the reaction heat Q of the device is obtained. R =Q2-Q1; the specific components include the sulfur content, nitrogen content and oxygen content of the feedstock oil.

[0086] S123. Arrange the contents of specific components of the multiple samples in ascending order, determine the reaction heat corresponding to the content of each specific component, and according to a curve graph corresponding to the reaction heat and the content of the specific component, select a fitting formula form that is closest to the curve graph according to curve fitting forms such as linear fitting, power function fitting, polynomial fitting (the highest number of polynomial fitting can be selected from 1 to 6 times, preferably 4 times), and establish correlation formulas between the reaction heat and the content of each specific component.

[0087] The correlation formula (Formula 1) between the reaction heat and the sulfur content of the feedstock oil can be:

[0088] Q 反 =a*(S in -S out ) / M oil，feed +e1;

[0089] The correlation formula (Formula 2) between the reaction heat and the nitrogen content of the feedstock oil can be:

[0090] Q 反 =b*(N in -N out ) / M oil，feed +e2;

[0091] The correlation formula (Formula 3) between the reaction heat and the oxygen content of the feedstock oil can be:

[0092] Q 反 =c*(O in -O out ) / M oil，feed +e3.

[0093] S124. After establishing the correlation formulas between the reaction heat and the sulfur content of the crude oil (Formula 1), the correlation formula between the reaction heat and the nitrogen content of the crude oil (Formula 2), and the correlation formula between the reaction heat and the oxygen content of the crude oil (Formula 3), respectively determine the reaction conversion rate and reaction heat of each sample in the data sample.

[0094] S125, replacing the specific components in step S122 and step S123 with reaction conversion rate, and establishing a correlation formula (Formula 4) between reaction heat and reaction conversion rate in the manner of step S122 and step S123:

[0095] Q 反 =d*K+e4;

[0096] In the above (Formula 1), (Formula 2), (Formula 3) and (Formula 4), Q 反 is the reference reaction heat per unit mass of crude oil; M oil，feed is the crude oil flow rate; S in S is the sulfur content of the raw oil at the reactor inlet; out is the sulfur content of the reaction effluent at the reactor outlet; N in N is the nitrogen content of the raw oil at the reactor inlet; out is the nitrogen content of the reaction effluent at the reactor outlet; in is the oxygen content of the raw oil at the reactor inlet; O out is the oxygen content of the reaction effluent at the reactor outlet; K is the conversion rate of the hydrocracking reaction; the preset coefficients include: a is the heat coefficient of the hydrodesulfurization reaction; b is the heat coefficient of the hydrodenitrogenation reaction; c is the heat coefficient of the hydrodeoxygenation reaction; d is the heat coefficient of the hydrocracking reaction; e1, e2, e3 and e4 are all constants related to the heat of the hydrocracking reaction (wherein the sum of e1, e2, e3 and e4 is e).

[0097] S126. Generate a mathematical correlation formula by adding the correlation formula between the reaction heat and the sulfur content of the feedstock oil, the correlation formula between the reaction heat and the nitrogen content of the feedstock oil, the correlation formula between the reaction heat and the oxygen content of the feedstock oil, and the correlation formula between the reaction heat and the reaction conversion rate. Among them, the reaction heat is the dependent variable, and the sulfur content of the feedstock oil, the nitrogen content of the feedstock oil, the oxygen content of the feedstock oil, and the reaction conversion rate are four independent variables corresponding to the dependent variable.

[0098] Furthermore, the mathematical correlation in step S126 may be further corrected by the following steps.

[0099] S127. Using the sample in the data sample as a parameter, generate an estimated value of the reaction heat according to the preliminary mathematical correlation formula; and using the reaction heat obtained according to the laboratory analysis data and the material balance calculation as a reference value, determine the relative error of each sample, which can be specifically:

[0100] Relative error = ABS (reference value - estimated value) / reference value; wherein ABS (reference value - estimated value) is the absolute value of the difference between the reference value and the estimated value.

[0101] S128. According to the relative error calculated in step S127, sample values ​​corresponding to relative errors exceeding 5% are eliminated to update the data samples.

[0102] S129, repeating steps S122 to S128 according to the updated data samples until the relative errors of the reaction heat sample values ​​are all within 5%, thereby obtaining the final mathematical correlation equation.

[0103] S13. According to the solution results of the preset coefficients, a calculation model suitable for the hydrocracking unit is constructed, wherein the calculation model includes the mathematical correlation formula into which the solution results of the preset coefficients are introduced.

[0104] The preset coefficients (including the hydrodesulfurization reaction heat coefficient a, the hydrodenitrogenation reaction heat coefficient b, the hydrodeoxygenation reaction heat coefficient c, the hydrocracking reaction heat coefficient d, and the hydrocracking reaction heat-related constant e) obtained by solving the above-mentioned mathematical correlation formula are only applicable to the hydrocracking unit for which data collection and analysis are performed above; that is, the hydrodesulfurization reaction heat coefficient a, the hydrodenitrogenation reaction heat coefficient b, the hydrodeoxygenation reaction heat coefficient c, the hydrocracking reaction heat coefficient d, and the hydrocracking reaction heat-related constant e in the embodiment of the present invention are not universal, but are obtained by performing data collection, analysis and calculation on a specific hydrocracking unit, and are only applicable to the hydrocracking unit.

[0105] By substituting the preset coefficients into the above mathematical correlation formula, a calculation model suitable for the hydrocracking unit can be generated, and the calculation model is used to calculate the current reaction heat of the hydrocracking unit; specifically, first, after substituting the preset coefficients into the above mathematical correlation formula, other parameters in the mathematical correlation formula, such as the sulfur, nitrogen, oxygen content and reaction conversion rate data of the feed oil and the produced oil can be obtained after data collection and analysis. In this way, the reaction heat of the hydrocracking unit under the current operating conditions can be calculated through the calculation model.

[0106] In summary, in the embodiment of the present invention, a mathematical correlation formula is first constructed to express the relationship between the data of the specific components such as sulfur content, nitrogen content and oxygen content in the raw oil at the reactor inlet and the reaction effluent at the reactor outlet and the reaction conversion rate and reaction heat. Then, the preset coefficients in the mathematical correlation formula are solved by performing data collection and analysis on the specific hydrocracking unit and calculating the reaction conversion rate and reaction heat, so as to generate a measurement model suitable for the specific hydrocracking unit. The measurement model in the embodiment of the present invention is generated based on multiple data collection, analysis and calculation of the raw oil and each product of the specific hydrocracking unit, so that the reaction heat of the specific hydrocracking unit can be accurately calculated based on the measured specific components.

[0107] As can be seen from the above, compared with the prior art method of obtaining the reaction heat by summing up various types of reaction heat such as hydrodenitrogenation reaction, hydrodesulfurization reaction, olefin hydrogenation reaction, aromatics saturation reaction, cycloalkane cracking reaction, and paraffin cracking, the embodiment of the present invention does not need to empirically estimate the number of different types of reactions occurring in the hydrocracking process and the values ​​of various types of reaction heat when measuring the reaction heat of a certain hydrocracking unit in real time, thereby effectively improving the accuracy of the reaction heat result value.

[0108] In addition, compared with another prior art method of measuring the combustion heat data of the feedstock oil and products of the hydrocracking unit in the laboratory and then calculating the difference in the combustion heat of the feedstock oil and the products to obtain the reaction heat, the embodiment of the present invention does not need to measure the accurate combustion heat data of the feedstock oil and each product when calculating the reaction heat of the hydrocracking unit, thereby reducing the dependence on experimental analysis and reducing the complexity and difficulty of calculating the reaction heat of the hydrocracking unit in actual production.

[0109] In the embodiment of the present invention, after the calculation model is generated, its specific application method may include:

[0110] S14, collecting and analyzing data on the current operating conditions of the hydrocracking unit to obtain data on the sulfur, nitrogen, and oxygen contents and reaction conversion rates of the feed oil and the produced oil;

[0111] When it is necessary to calculate the current reaction heat of the hydrocracking unit corresponding to the calculation model, it is first necessary to obtain the sulfur, nitrogen, oxygen content and reaction conversion rate data of the feed oil and the produced oil after data collection and analysis under the current operating conditions.

[0112] S15. Calculate the reaction heat of the hydrocracking unit according to the calculation model.

[0113] In the calculation model in the embodiment of the present invention, the preset coefficients of the mathematical correlation are all known, that is, the hydrodesulfurization reaction heat coefficient a, the hydrodenitrogenation reaction heat coefficient b, the hydrodeoxygenation reaction heat coefficient c, the hydrocracking reaction heat coefficient d, and the hydrocracking reaction heat related constant e are all known; at this time, after adding the reaction conversion rate that can be obtained by calculation, the only unknown number in the mathematical correlation (that is, the reaction heat) can be calculated.

[0114] Embodiment 2

[0115] In another aspect of the embodiment of the present invention, Figure 2 As shown, based on the first embodiment, a method for optimizing energy consumption of a hydrocracking unit is also provided, comprising the steps of:

[0116] S21, firstly, generating a calculation model of a hydrocracking unit according to the reaction heat calculation method of a hydrocracking unit in Example 1;

[0117] In this embodiment of the present invention, it is also necessary to generate the same mathematical correlation as in the above-mentioned embodiment 1. The mathematical correlation is used to express the relationship between the data of specific components such as sulfur content, nitrogen content and oxygen content in the raw oil at the reactor inlet and the reaction effluent at the reactor outlet and the reaction conversion rate and reaction heat. The specific method of generating the mathematical correlation can refer to the corresponding record in embodiment 1.

[0118] Then, according to the mathematical correlation formula, by solving the above-mentioned preset coefficients (including the hydrodesulfurization reaction heat coefficient a, the hydrodenitrogenation reaction heat coefficient b, the hydrodeoxygenation reaction heat coefficient c, the hydrocracking reaction heat coefficient d, and the hydrocracking reaction heat-related constant e), a calculation model corresponding to the hydrocracking unit is generated; the specific generation method of the calculation model can refer to the description in Example 1.

[0119] S22, generating an objective function for energy consumption optimization according to the mathematical correlation in the calculation model; the objective function aims to maximize the reaction heat calculation result, and the objective function includes:

[0120] maxf=a*(S in -S out ) / M oil，feed +b*(N in -N out ) / M oil，feed +c*(O in -O out ) / M oil，feed +d*K+e

[0121] Wherein, maxf is the result of reaction heat calculation; S in S is the sulfur content of the raw oil at the reactor inlet; outis the sulfur content of the reaction effluent at the reactor outlet; N in N is the nitrogen content of the raw oil at the reactor inlet; out is the nitrogen content of the reaction effluent at the reactor outlet; in is the oxygen content of the raw oil at the reactor inlet; O out is the oxygen content of the reaction effluent at the reactor outlet; K is the conversion rate of the hydrocracking reaction; the preset coefficients include: a is the heat coefficient of the hydrodesulfurization reaction; b is the heat coefficient of the hydrodenitrogenation reaction; c is the heat coefficient of the hydrodeoxygenation reaction; d is the heat coefficient of the hydrocracking reaction; e is the heat-related constant of the hydrocracking reaction;

[0122] Different from the first embodiment, the embodiment of the present invention constructs an objective function for determining the optimal value of the reaction heat based on the measurement model.

[0123] S23, adjusting the content composition of sulfur, nitrogen and oxygen in the crude oil, and / or adjusting the processing conversion depth, and obtaining an optimization scheme for the content composition of sulfur, nitrogen and oxygen in the crude oil and the processing conversion depth according to the objective function;

[0124] The constraints of the objective function include:

[0125] 0≤S in ≤S max ; 0≤N in ≤N max ; 0≤O in ≤O max ;

[0126] Among them, S in is the sulfur content of the crude oil after mixing feeds from various sources, N in is the nitrogen content of the crude oil after mixing feeds from multiple sources, O in It is the oxygen content of the raw oil after mixing feeds from multiple sources.

[0127] In the embodiment of the present invention, reasonable ranges of sulfur content, nitrogen content and oxygen content of the feedstock oil are set respectively; and the optimization scheme of the content composition of sulfur, nitrogen and oxygen in the feedstock oil and the processing conversion depth is obtained through the objective function with the reasonable range as a constraint condition; specifically, the different combinations of various sulfur contents, nitrogen contents and oxygen contents can be respectively solved by the objective function to obtain the corresponding reaction heat results, and then the optimal content composition of sulfur, nitrogen and oxygen in the feedstock oil and the processing conversion depth and other data are determined according to the optimal solution (or the solution that meets the preset standard), and then the corresponding optimization scheme can be generated.

[0128] In practical applications, the temperature rise of the bed at the end of the hydrocracking reactor can also be used as a constraint condition of the objective function. Specifically:

[0129] The constraints of the objective function also include:

[0130]

[0131] Where, ΔT b is the temperature rise of the bed at the end of the hydrocracking reactor; It is the minimum temperature rise of the bed at the end of the hydrocracking reactor, which is determined according to the production requirements of the hydrocracking unit; It is the maximum allowable temperature rise of the bed at the end of the hydrocracking reactor, which is determined based on the design data of the hydrocracking reactor and / or the requirements of the on-site device generation.

[0132] Among them, the method for calculating the temperature rise of the bed at the end of the hydrocracking reactor can be:

[0133] Obtaining the reaction conversion rate of the hydrocracking unit;

[0134] The temperature rise of the bed at the end of the hydrocracking reactor is calculated according to the corresponding relationship between the reaction conversion rate of the hydrocracking unit and the temperature rise of the bed at the end of the hydrocracking reactor;

[0135] The corresponding relationship includes: K = f(ΔT b );

[0136] Where, ΔT b is the bed temperature rise at the end of the hydrocracking reactor; K is the reaction conversion rate of the hydrocracking unit.

[0137] In summary, in the embodiments of the present invention, a mathematical correlation formula is first constructed to express the relationship between the data of specific components such as sulfur content, nitrogen content and oxygen content in the raw oil at the reactor inlet and the reaction effluent at the reactor outlet and the reaction conversion rate and reaction heat. Then, the preset coefficients in the mathematical correlation formula are solved by performing data collection and analysis on the specific hydrocracking unit and calculating the reaction conversion rate and reaction heat, so as to generate a measurement model suitable for the specific hydrocracking unit.

[0138] The calculation model in the embodiment of the present invention is generated based on multiple data collection, analysis and calculation of the feedstock oil and each product of a specific hydrocracking unit, and can accurately calculate the reaction heat of the specific hydrocracking unit according to the composition of the specific components. In view of this, the inventor constructed an objective function for obtaining the optimal solution for the reaction heat based on the calculation model, and determined the content composition combination of the specific components in the feedstock oil when the optimal reaction heat can be obtained from the reaction heat calculation results obtained by the different content composition combinations of the specific components of the feedstock oil, thereby being able to generate an optimization plan for guiding the optimization of the production process of the hydrocracking unit.

[0139] The method for calculating the reaction heat of a hydrocracking unit in an embodiment of the present invention proposes a method for calculating and predicting the reaction heat of a hydrocracking unit based on the properties of the raw materials and the reaction conversion rate. The calculation is simple and reliable. The change in the reaction heat of the hydrocracking unit for different feeds can be known in advance, thereby guiding the operator of the hydrocracking unit to adjust the relevant process parameters and the heat exchange network; from the perspective of maximizing the reaction heat, while meeting the raw material properties and product requirements of the unit, the reaction heat of the unit is maximized through raw material adjustment and process parameter adjustment, thereby using heat for raw material heat exchange to reduce the fuel consumption of the heating furnace, giving full play to the potential for optimizing energy saving of the entire hydrocracking system, and effectively improving the energy consumption level of the system, and reducing the energy consumption and production cost of the unit.

[0140] The beneficial effects of the embodiments of the invention (including Embodiment 1 and Embodiment 2) are described below by comparative examples:

[0141] By sampling the crude oil and products, the distillation range, composition, density and other analytical data of the crude oil and products are obtained by mass spectrometry, chromatography and nuclear magnetic resonance analysis methods, as shown in Table 1 and Table 2;

[0142] Table 1: Raw oil and product properties

[0143] project Crude oil Light naphtha Heavy naphtha Jet fuel diesel fuel tail oil <![CDATA[Density kg / m 3 > 906.1 629.7 749.3 805.3 818.1 827.6 Initial distillation point ℃ 203.5 23.0 85.0 152.0 217.0 198.0 10％ ℃ 340.0 28.0 99.0 173.0 248.0 296.0 30％ ℃ 374.5 33.0 104.0 189.3139 274.0 343.0 50％ ℃ 404.5 39.0 118.0 203.0 289.0 371.0 70％ ℃ 435.0 47.0 132.0 218.0315 300.0 394.0 90％ ℃ 467.5 58.0 149.0 240 315.0 441.0 Dry point℃ 503.0 68.0 171.0 262.0 331.0 469.0 S ppm 23230 10 0.52 10 10 10 N ppm 507 0.3 0.58 0.3 0.31 0.62

[0144] Table 2: Gas composition

[0145] project unit New Hydrogen Cyclic Hydrogen Low gas Dry gas Liquefied gas hydrogen ％ 96.07 84.59 68.59 27.66 0 Methane ％ 1.66 9.77 12.14 40.31 0 Ethane ％ 1.23 2.67 5.39 20.14 0 Propane ％ 0.77 1.41 3.35 3.83 35.79 n-Butane ％ 0.08 0.84 1.89 0.46 41.06 Isobutane ％ 0.17 0.38 0.89 0.04 22.57 C5 and above ％ 0 0.3 0.81 0.04 0.58

[0146] Next, the material balance of the hydrocracking unit was calculated by the feedstock oil, the newly added hydrogen, and the flow rates of the liquid and gas products. The results are shown in Table 3.

[0147] Table 3: Material balance

[0148]

[0149] According to the calculation method of calculating the reaction heat according to the elemental analysis of the feed oil and the hydrogenated product oil and the empirical formula of the combustion heat in the prior art (in the embodiment of the present invention, the improved Riazi method proposed by Riazi MR is taken as an example), the carbon and hydrogen elemental analysis of the feed oil and the product oil is obtained as shown in Table 4;

[0150] Table 4: Elemental analysis of crude oil and hydrogenated oil

[0151]

[0152] The specific calculation methods include:

[0153] The calculation formula for heat of generation is as follows:

[0154] QF =(78.29×C+338.85×H+22.2×S-42.7×O)-Q c

[0155] The formula for calculating the high calorific value of combustion heat is as follows

[0156] Q c =81×C+300×H-26(OS)

[0157] Wherein, C, H, S, O are the mass fractions of carbon, hydrogen, sulfur and oxygen in the feed oil or produced oil, respectively.

[0158] Reaction heat Q R The calculation formula is: Q R = heat of formation of generated oil + heat of formation of generated gas - heat of formation of reaction products; wherein, the heat of formation of each component of generated gas can be found in the petrochemical data manual.

[0159] The reaction heat calculation result obtained by the reaction heat calculation method of the hydrocracking unit according to the embodiment of the present invention is referred to as Comparative Example 1 in the embodiment of the present invention.

[0160] The calculation method used for accuracy comparison with the embodiments of the present invention is the calculation method of the reaction heat according to the elemental analysis of the feed oil and the hydrogenated oil and the empirical formula for the combustion heat corresponding to the above Table 4; the reaction heat calculation result is referred to as Comparative Example 2 in the embodiments of the present invention.

[0161] In the embodiment of the present invention, the benchmark for measuring whether the reaction heat calculation result is accurate is: based on material balance, laboratory analysis data, and device process operation parameters, using process simulation software such as Aspen Plus, Aspen Hysys, and Pro-Ⅱ, select a suitable state equation. According to the temperature and pressure parameters of the reactor inlet raw oil, circulating hydrogen, new hydrogen, and cold hydrogen, the total input heat Q1 of the reactor inlet reaction flow is obtained; according to the temperature and pressure parameters of the reactor outlet circulating hydrogen, low-fraction gas, gas phase product, and liquid phase product, the total input heat Q2 of the reactor outlet reaction effluent is obtained, and the reaction heat Q of the device is obtained. R =Q2-Q1. The reaction heat calculation result is referred to as Comparative Example 3 in the examples of the present invention.

[0162] In addition, after optimizing the optimization scheme obtained by the method for optimizing the energy consumption of a hydrocracking unit in the embodiment of the present invention, the reaction heat calculation result obtained is referred to as Comparative Example 4 in the embodiment of the present invention.

[0163] Table 5: Comparative data of calculation results of Comparative Examples 1 to 4

[0164] project unit Comparative Example 1 Comparative Example 2 Comparative Example 3 After optimization Reaction heat kJ / kg 535.51 461.99 567.99 545.26 Temperature rise of the bed at the end of the hydrocracking reactor ℃ 12 12 12 15 Volume conversion rate ％ 71.32 71.32 71.32 71.51 Sulfur content of raw materials ％ 2.32 2.32 2.32 2.5 Nitrogen content of raw materials ％ 0.05 0.05 0.05 0.07 Raw material oxygen content ％ 0 0 0 0

[0165] As can be seen from Table 5, taking the reaction heat calculated by large-scale process simulation software in Comparative Example 3 as a benchmark, the reaction heat obtained by calculating the reaction heat according to the elemental analysis of the feed oil and the hydrogenated oil and the empirical formula of the combustion heat in Comparative Example 2 is quite different from the benchmark value. Comparative Example 1 is the reaction heat obtained by the reaction heat measurement method in the embodiment of the present invention (Example 1), and its result is close to the benchmark value, indicating that the embodiment of the present invention has good extrapolation and can be used as a prediction tool for the reaction heat of the hydrogenation process; further, according to the optimization scheme in the embodiment of the present invention (Example 2), it can also provide guidance for operators of oil refineries to adjust the heat exchange network to reduce the energy consumption of the device.

[0166] Embodiment 3

[0167] In another aspect of the embodiment of the present invention, a device for calculating reaction heat of a hydrocracking unit is also provided. Figure 3 The schematic diagram of the structure of the reaction heat calculation device of the hydrocracking unit provided in the embodiment of the present invention is shown. The reaction heat calculation device of the hydrocracking unit is Figure 1 The device corresponding to the method for calculating the reaction heat of the hydrocracking unit described in the corresponding embodiment, that is, the virtual device is used to realize Figure 1 In the corresponding embodiment, the method for calculating the reaction heat of a hydrocracking unit, each virtual module constituting the device for calculating the reaction heat of a hydrocracking unit can be executed by an electronic device, such as a network device, a terminal device, or a server. Specifically, the device for calculating the reaction heat of a hydrocracking unit in the embodiment of the present invention includes:

[0168] The data acquisition and analysis unit 01 is used to perform data acquisition and analysis on the hydrocracking unit under different working conditions. The content of each data acquisition and analysis includes: obtaining the test analysis data of the raw materials and products of the hydrocracking unit; calculating the reaction conversion rate of the hydrocracking unit; calculating the reference reaction heat of the hydrocracking unit;

[0169] The coefficient solving unit 02 is used to respectively bring the sulfur, nitrogen, oxygen content, reaction conversion rate and reference reaction heat data of the feedstock oil and the produced oil obtained by data collection and analysis of the hydrocracking unit into a preset mathematical correlation formula to solve the preset coefficients of the mathematical correlation formula; the mathematical correlation formula includes:

[0170] Q 反 =a*(S in -S out ) / M oil，feed +b*(N in -N out ) / M oil，feed +c*(O in -O out ) / Moil，feed +d*K+e

[0171] Among them, Q 反 is the reference reaction heat per unit mass of crude oil; S in S is the sulfur content of the raw oil at the reactor inlet; out is the sulfur content of the reaction effluent at the reactor outlet; N in N is the nitrogen content of the raw oil at the reactor inlet; out is the nitrogen content of the reaction effluent at the reactor outlet; in is the oxygen content of the raw oil at the reactor inlet; O out is the oxygen content of the reaction effluent at the reactor outlet; K is the conversion rate of the hydrocracking reaction; the preset coefficients include: a is the heat coefficient of the hydrodesulfurization reaction; b is the heat coefficient of the hydrodenitrogenation reaction; c is the heat coefficient of the hydrodeoxygenation reaction; d is the heat coefficient of the hydrocracking reaction; e is the heat-related constant of the hydrocracking reaction;

[0172] The calculation model construction unit 03 is used to construct a calculation model suitable for the hydrocracking unit according to the solution results of the preset coefficients, and the calculation model includes the mathematical correlation formula with the solution results of the preset coefficients.

[0173] Furthermore, in the embodiment of the present invention, the following may also be included:

[0174] Real-time data acquisition unit 04, used to acquire sulfur, nitrogen, oxygen content and reaction conversion rate data of feed oil and produced oil after data acquisition and analysis under current operating conditions of the hydrocracking unit;

[0175] The result generating unit 05 is used to calculate and obtain the reaction heat of the hydrocracking unit according to the calculation model.

[0176] Since the working principle and beneficial effects of the reaction heat calculation device for the hydrocracking unit in the embodiment of the present invention have been Figure 1 The corresponding method for calculating the heat of reaction of the hydrocracking unit is also recorded and described, so they can be cross-referenced and will not be repeated here.

[0177] Embodiment 4

[0178] In an embodiment of the present invention, a memory is further provided, wherein the memory includes a software program, and the software program is suitable for the processor to execute Figure 1 The corresponding steps in the method for calculating the reaction heat of a hydrocracking unit, or suitable for the processor to execute Figure 2 The corresponding steps in the energy consumption optimization method of the hydrocracking unit.

[0179] The embodiments of the present invention can be implemented by means of a software program, that is, by writing a program for implementing Figure 1The corresponding steps in the method for calculating the heat of reaction of the hydrocracking unit, or, Figure 2 The corresponding software program (and instruction set) for each step in the method for optimizing energy consumption of a hydrocracking unit is stored in a storage device, which is arranged in a computer device, so that the software program can be called by the processor of the computer device to achieve the purpose of the embodiment of the present invention.

[0180] Embodiment 4

[0181] In an embodiment of the present invention, a device for calculating the reaction heat of a hydrocracking unit is also provided. The memory included in the device for calculating the reaction heat of a hydrocracking unit includes a corresponding computer program product. When the program instructions included in the computer program product are executed by a computer, the computer can execute the method for calculating the reaction heat of a hydrocracking unit described in the above aspects and achieve the same technical effect.

[0182] Figure 4 Schematic diagram of the hardware structure of the reaction heat calculation device of the hydrocracking unit as an electronic device in an embodiment of the present invention, such as Figure 4 As shown, the device includes one or more processors 610, a bus 630, and a memory 620. Taking one processor 610 as an example, the device may also include: an input device 640, and an output device 650.

[0183] The processor 610, the memory 620, the input device 640 and the output device 650 may be connected via a bus or other means. Figure 4 The example of connecting through bus is taken in the following.

[0184] The memory 620 is a non-transitory computer-readable storage medium that can be used to store non-transitory software programs, non-transitory computer executable programs, and modules. The processor 610 executes various functional applications and data processing of the electronic device by running the non-transitory software programs, instructions, and modules stored in the memory 620, that is, the processing method of the above method embodiment is implemented.

[0185] The memory 620 may include a program storage area and a data storage area, wherein the program storage area may store an operating system, an application required for at least one function; the data storage area may store data, etc. In addition, the memory 620 may include a high-speed random access memory, and may also include a non-transitory memory, such as at least one disk storage device, a flash memory device, or other non-transitory solid-state storage device. In some embodiments, the memory 620 may optionally include a memory remotely arranged relative to the processor 610, and these remote memories may be connected to the processing device via a network. Examples of the above-mentioned network include, but are not limited to, the Internet, an intranet, a local area network, a mobile communication network, and combinations thereof.

[0186] The input device 640 can receive input digital or character information and generate signal input. The output device 650 can include a display device such as a display screen.

[0187] The one or more modules are stored in the memory 620, and when executed by the one or more processors 610, perform:

[0188] S11, respectively collecting and analyzing data on the hydrocracking unit under different working conditions, wherein the content of each data collection and analysis includes: obtaining the test analysis data of the raw materials and products of the hydrocracking unit; calculating the reaction conversion rate of the hydrocracking unit; calculating the reference reaction heat of the hydrocracking unit;

[0189] S12, respectively bringing the sulfur content, nitrogen content, oxygen content, reaction conversion rate and reference reaction heat data of the feed oil and the produced oil obtained by data collection and analysis of the hydrocracking unit into a preset mathematical correlation formula, and solving the preset coefficients of the mathematical correlation formula; the mathematical correlation formula includes:

[0190] Q 反 =a*(S in -S out ) / M oil，feed +b*(N in -N out ) / M oil，feed +c*(O in -O out ) / M oil，feed +d*K+e

[0191] Among them, Q 反 is the reference reaction heat per unit mass of crude oil; M oil，feed is the crude oil flow rate; S in S is the sulfur content of the raw oil at the reactor inlet; out is the sulfur content of the reaction effluent at the reactor outlet; N in N is the nitrogen content of the raw oil at the reactor inlet; out is the nitrogen content of the reaction effluent at the reactor outlet; in is the oxygen content of the raw oil at the reactor inlet; O out is the oxygen content of the reaction effluent at the reactor outlet; K is the conversion rate of the hydrocracking reaction; the preset coefficients include: a is the heat coefficient of the hydrodesulfurization reaction; b is the heat coefficient of the hydrodenitrogenation reaction; c is the heat coefficient of the hydrodeoxygenation reaction; d is the heat coefficient of the hydrocracking reaction; e is the heat-related constant of the hydrocracking reaction;

[0192] S13. According to the solution results of the preset coefficients, a calculation model suitable for the hydrocracking unit is constructed, wherein the calculation model includes the mathematical correlation formula into which the solution results of the preset coefficients are introduced.

[0193] Furthermore, in the embodiment of the present invention, the steps may also be included:

[0194] S14, the sulfur, nitrogen, oxygen content and reaction conversion rate data of the feed oil and the produced oil obtained after data collection and analysis under the current operating conditions of the hydrocracking unit;

[0195] S15. Calculate the reaction heat of the hydrocracking unit according to the calculation model.

[0196] The above product can execute the method provided by the embodiment of the present invention, and has the functional modules and beneficial effects corresponding to the execution method. For technical details not described in detail in this embodiment, please refer to the method provided by the embodiment of the present invention.

[0197] In the several embodiments provided by the present invention, it should be understood that the disclosed systems, devices and methods can be implemented in other ways. For example, the device embodiments described above are only schematic. For example, the division of the units is only a logical function division. There may be other division methods in actual implementation, such as multiple units or components can be combined or integrated into another system, or some features can be ignored or not executed. Another point is that the mutual coupling or direct coupling or communication connection shown or discussed can be an indirect coupling or communication connection through some interfaces, devices or units, which can be electrical, mechanical or other forms.

[0198] The units described as separate components may or may not be physically separated, and the components shown as units may or may not be physical units, that is, they may be located in one place or distributed on multiple network units. Some or all of the units may be selected according to actual needs to achieve the purpose of the solution of this embodiment.

[0199] In addition, each functional unit in each embodiment of the present invention may be integrated into one processing unit, or each unit may exist physically separately, or two or more units may be integrated into one unit. The above-mentioned integrated unit may be implemented in the form of hardware or in the form of software functional units.

[0200] If the integrated unit is implemented in the form of a software functional unit and sold or used as an independent product, it can be stored in a computer-readable storage medium. Based on this understanding, the technical solution of the present invention is essentially or the part that contributes to the prior art or all or part of the technical solution can be embodied in the form of a software product. The computer software product is stored in a storage device, including several instructions to enable a computer device (which can be a personal computer, server, or network device, etc.) to perform all or part of the steps of the method described in each embodiment of the present invention. The aforementioned storage device includes: U disk, mobile hard disk, read-only memory (ROM, Read-Only Memory), random access memory (RAM, Random Access Memory), ReRAM, MRAM, PCM, NAND Flash, NOR Flash, Memristor, disk or optical disk and other media that can store program codes.

[0201] As described above, the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit the same. Although the present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that the technical solutions described in the aforementioned embodiments may still be modified, or some of the technical features thereof may be replaced by equivalents. However, these modifications or replacements do not deviate the essence of the corresponding technical solutions from the spirit and scope of the technical solutions of the embodiments of the present invention.

Claims

1. A method for calculating the heat of reaction of a hydrocracking unit, characterized in that: Includes steps: S11, respectively collecting and analyzing data on the hydrocracking unit under different working conditions, wherein the content of each data collection and analysis includes: obtaining the test analysis data of the raw materials and products of the hydrocracking unit; calculating the reaction conversion rate of the hydrocracking unit; calculating the reference reaction heat of the hydrocracking unit; S12, respectively bringing the sulfur content, nitrogen content, oxygen content, reaction conversion rate and reference reaction heat data of the feed oil and the produced oil obtained by data collection and analysis of the hydrocracking unit into a preset mathematical correlation formula, and solving the preset coefficients of the mathematical correlation formula; the mathematical correlation formula includes: Q 反 =a*(S in -S out ) / M oil，feed +b*(N in -N out ) / M oil,feed +c*(O in -O out) / M oil，feed +d*K+e Among them, Q 反 is the reference reaction heat per unit mass of crude oil; M oil，feed is the crude oil flow rate; S in S is the sulfur content of the raw oil at the reactor inlet; out is the sulfur content of the reaction effluent at the reactor outlet; N in N is the nitrogen content of the raw oil at the reactor inlet; out is the nitrogen content of the reaction effluent at the reactor outlet; in is the oxygen content of the raw oil at the reactor inlet; O out is the oxygen content of the reaction effluent at the reactor outlet; K is the conversion rate of the hydrocracking reaction; the preset coefficients include: a is the heat coefficient of the hydrodesulfurization reaction; b is the heat coefficient of the hydrodenitrogenation reaction; c is the heat coefficient of the hydrodeoxygenation reaction; d is the heat coefficient of the hydrocracking reaction; e is the heat-related constant of the hydrocracking reaction; S13. According to the solution results of the preset coefficients, a calculation model suitable for the hydrocracking unit is constructed, wherein the calculation model includes the mathematical correlation formula into which the solution results of the preset coefficients are introduced.

2. The method for calculating the reaction heat of a hydrocracking unit according to claim 1, characterized in that: Also includes: S14, collecting and analyzing data on the current operating conditions of the hydrocracking unit to obtain data on the sulfur, nitrogen, and oxygen contents and reaction conversion rates of the feed oil and the produced oil; S15. Calculate the reaction heat of the hydrocracking unit according to the calculation model.

3. The method for calculating the reaction heat of a hydrocracking unit according to claim 1, characterized in that: The laboratory analysis data at least include distillation range, components and density; the components at least include sulfur content, nitrogen content and oxygen content.

4. The method for calculating the reaction heat of a hydrocracking unit according to claim 1, characterized in that: The calculation to obtain the reference reaction heat of the hydrocracking unit includes: Carrying out material balance accounting for the hydrocracking unit through the flow of raw oil, new hydrogen supplementation, and liquid and gas products; The applicable state equation is determined based on material balance, laboratory analysis data and process operation parameters of the hydrocracking unit; and the reference reaction heat of the hydrocracking unit is obtained according to the total input heat of the reactor inlet reactant flow and the total input heat of the reactor outlet reaction effluent.

5. The method for calculating the reaction heat of a hydrocracking unit according to claim 4, characterized in that: The method of determining the applicable state equation based on material balance, laboratory analysis data and process operation parameters of the hydrocracking unit includes: Based on material balance, laboratory analysis data and process operating parameters of the hydrocracking unit, an applicable state equation is determined using Aspen Plus, Aspen Hysys or Pro-II process simulation software.

6. The method for calculating the reaction heat of a hydrocracking unit according to claim 4, characterized in that: The step of obtaining the reference reaction heat of the hydrocracking unit according to the total input heat of the reactor inlet reactant stream and the total input heat of the reactor outlet reaction effluent comprises: According to the temperature and pressure parameters of the raw oil, circulating hydrogen, new hydrogen and cold hydrogen at the reactor inlet, the total input heat Q1 of the reactor inlet reactant flow is obtained; according to the temperature and pressure parameters of the circulating hydrogen, low-fraction gas, gas phase product and liquid phase product at the reactor outlet, the total input heat Q2 of the reactor outlet reaction effluent is obtained, and the reference reaction heat Q of the device is obtained. R =Q 2- Q1.

7. The method for calculating the reaction heat of a hydrocracking unit according to claim 1, characterized in that: The formula for calculating the reaction conversion rate of the hydrocracking unit includes: Reaction conversion rate = 100% * (fraction > 350°C in the feed oil - fraction > 350°C in the product oil) / fraction > 350°C in the feed oil.

8. The method for calculating the reaction heat of a hydrocracking unit according to claim 1, characterized in that: The hydrocracking unit comprises: Wax oil hydrocracking unit, diesel hydrocracking unit, high pressure hydrocracking unit or medium pressure hydrocracking unit.

9. A method for optimizing energy consumption of a hydrocracking unit, characterized in that: include: S21. generating a calculation model of the hydrocracking unit according to the method for calculating reaction heat of the hydrocracking unit as claimed in any one of claims 1 to 8; S22, generating an objective function for energy consumption optimization according to the mathematical correlation in the calculation model; the objective function aims to maximize the reaction heat calculation result, and the objective function includes: maxf=a*(S in -S out ) / M oil，feed +b*(N in -N out ) / M oil，feed +c*(O in -O out ) / M oil，feed +d*K+e Wherein, maxf is the result of reaction heat calculation; S in S is the sulfur content of the raw oil at the reactor inlet; out is the sulfur content of the reaction effluent at the reactor outlet; N in N is the nitrogen content of the raw oil at the reactor inlet; out is the nitrogen content of the reaction effluent at the reactor outlet; in is the oxygen content of the raw oil at the reactor inlet; O out is the oxygen content of the reaction effluent at the reactor outlet; K is the conversion rate of the hydrocracking reaction; the preset coefficients include: a is the heat coefficient of the hydrodesulfurization reaction; b is the heat coefficient of the hydrodenitrogenation reaction; c is the heat coefficient of the hydrodeoxygenation reaction; d is the heat coefficient of the hydrocracking reaction; e is the heat-related constant of the hydrocracking reaction; S23, adjusting the sulfur content, nitrogen content, and oxygen content composition of the feedstock oil, and / or adjusting the processing conversion depth, and obtaining an optimization scheme for the sulfur content, nitrogen content, and oxygen content composition of the feedstock oil and the processing conversion depth according to the objective function; The constraints of the objective function include: 0≤S in ≤S max ;0≤N in ≤N max ;0≤O in ≤O max ; Among them, S in is the sulfur content of the crude oil after mixing feeds from various sources, N in is the nitrogen content of the crude oil after mixing feeds from multiple sources, O in It is the oxygen content of the raw oil after mixing feeds from multiple sources.

10. The method for optimizing energy consumption of a hydrocracking unit according to claim 9, characterized in that: The constraints of the objective function also include: Where, ΔT b is the temperature rise of the bed at the end of the hydrocracking reactor; It is the minimum temperature rise of the bed at the end of the hydrocracking reactor, which is determined according to the production requirements of the hydrocracking unit; It is the maximum allowable temperature rise of the bed at the end of the hydrocracking reactor, which is determined based on the design data of the hydrocracking reactor and / or the requirements of the on-site device generation.

11. The method for optimizing energy consumption of a hydrocracking unit according to claim 10, characterized in that: Calculate the temperature rise of the bed at the end of the hydrocracking reactor, including: Obtaining the reaction conversion rate of the hydrocracking unit; Calculating the bed temperature rise at the end of the hydrocracking reactor according to the corresponding relationship between the reaction conversion rate of the hydrocracking unit and the bed temperature rise at the end of the hydrocracking reactor; The corresponding relationship includes: K = f(ΔT b ); Where, ΔT b is the bed temperature rise at the end of the hydrocracking reactor; K is the reaction conversion rate of the hydrocracking unit.

12. A device for calculating the heat of reaction of a hydrocracking unit, characterized in that: include: The data acquisition and analysis unit is used to collect and analyze data of the hydrocracking unit under different working conditions. The content of each data acquisition and analysis includes: obtaining the test analysis data of the raw materials and products of the hydrocracking unit; calculating the reaction conversion rate of the hydrocracking unit; calculating the reference reaction heat of the hydrocracking unit; The coefficient solving unit is used to respectively bring the sulfur content, nitrogen content, oxygen content, reaction conversion rate and reference reaction heat data of the feedstock oil and the generated oil obtained by data collection and analysis of the hydrocracking unit into a preset mathematical correlation formula to solve the preset coefficients of the mathematical correlation formula; the mathematical correlation formula includes: Q 反 =a*(S in -S out ) / M oil,feed +b*(N in -N out ) / M oil，feed +c*(O in -O out ) / M oil，feed +d*K+e Among them, Q 反 is the reference reaction heat per unit mass of crude oil; M oil，feed is the crude oil flow rate; S in S is the sulfur content of the raw oil at the reactor inlet; out is the sulfur content of the reaction effluent at the reactor outlet; N in N is the nitrogen content of the raw oil at the reactor inlet; out is the nitrogen content of the reaction effluent at the reactor outlet; in is the oxygen content of the raw oil at the reactor inlet; O out is the oxygen content of the reaction effluent at the reactor outlet; K is the conversion rate of the hydrocracking reaction; the preset coefficients include: a is the heat coefficient of the hydrodesulfurization reaction; b is the heat coefficient of the hydrodenitrogenation reaction; c is the heat coefficient of the hydrodeoxygenation reaction; d is the heat coefficient of the hydrocracking reaction; e is the heat-related constant of the hydrocracking reaction; The calculation model construction unit is used to construct a calculation model suitable for the hydrocracking unit according to the solution results of the preset coefficients, and the calculation model includes the mathematical association formula that incorporates the solution results of the preset coefficients.

13. A memory, characterized in that: The method comprises a software program, wherein the software program is suitable for executing the steps of the method for estimating reaction heat of a hydrocracking unit according to any one of claims 1 to 8 by a processor.

14. A hydrocracking unit reaction heat calculation device, characterized in that: comprising a bus, a processor and a memory as claimed in claim 13; The bus is used to connect the memory and the processor; The processor is configured to execute an instruction set in the memory.

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