Method and device for determining hydrogen transmission quantity of slurry reactor heavy oil micro-interface strengthening reaction and electronic equipment

Abstract

The invention provides a method and device for determining the hydrogen transmission amount of a slurry bed heavy oil micro-interface strengthening reaction and electronic equipment, and creatively establishes a physical model of a slurry bed heavy oil hydrogenation micro-interface reactor micro-interface unit which is suitable for pure pneumatic operation conditions and also suitable for pure hydraulic or gas-liquid linkage conditions. A mathematical model of the energy dissipation rate is deduced based on the physical model, so that the bubble size d32 and the micro-bubble average rising speed v32 of the micro-interface system can be further calculated based on the mathematical model of the energy dissipation rate, and then the hydrogen transmission amount is calculated. The scheme is suitable for pure pneumatic operation conditions, is also suitable for pure hydraulic or gas-liquid linkage conditions, is wide in application range, and can be widely used for guiding the design of the slurry bed heavy oil hydrogenation micro-interface reactor and the design of a reaction system of the slurry bed heavy oil hydrogenation micro-interface reactor.

Description

Technical Field

[0001] This application relates to the field of heavy oil hydrogenation technology, and in particular to a method, apparatus and electronic equipment for determining hydrogen transport capacity in a slurry bed heavy oil micro-interface enhanced reaction. Background Technology

[0002] The amount of hydrogen transported during the residence time of hydrogen bubbles in a heavy oil system is a key parameter determining the reaction efficiency of heavy oil. Hydrogen transport in heavy oil is generally considered to be determined by both Henry's Law and Fick's Law. However, the hydrogen transport process in a heavy oil hydrotreating micro-interface reactor system has not been reported. Therefore, it is necessary to establish a model to analyze hydrogen transport within a heavy oil hydrotreating reactor, thereby providing guidance for the design of slurry-bed heavy oil micro-interface enhanced reactors and the design of their reaction systems.

[0003] Existing technologies have proposed a modeling method for hydrogen transport regulation under pure pneumatic operation conditions in MIHA reactors. This method considers the influence of two hydrogen transport mechanisms on the amount of hydrogen transported. The established model comprehensively reflects the influence of reactor structure, system properties, and operating parameters on hydrogen transport. It can be used to predict the change of hydrogen transport as reactor design parameters change, which is beneficial for the design and scale-up of MIHA reactors.

[0004] However, this existing technology is only applicable to purely pneumatic operating conditions and not to purely hydraulic or pneumatic-hydraulic linkage conditions. Summary of the Invention

[0005] This specification provides a method, apparatus, and electronic equipment for determining hydrogen transport capacity in a slurry bed heavy oil micro-interface enhanced reaction, in order to address the problem of the narrow applicability of existing technologies.

[0006] To address the aforementioned technical problems, this specification provides a method for determining the hydrogen transport capacity of a slurry-bed heavy oil micro-interface enhanced reaction, comprising: acquiring reactor structural parameters, system physical property parameters, and operating parameters for the slurry-bed heavy oil micro-interface enhanced reaction; calculating the energy dissipation rate based on the reactor structural parameters, system physical property parameters, and operating parameters; calculating the bubble size based on the energy dissipation rate; calculating the rising velocity of a single bubble in an infinitely large static liquid phase based on the bubble size; calculating the average rising velocity of microbubbles in the micro-interface system based on the rising velocity of a single bubble in the infinitely large static liquid phase; and calculating the hydrogen transport capacity of the slurry-bed heavy oil micro-interface enhanced reaction based on the average rising velocity of microbubbles in the micro-interface system and the bubble size.

[0007] In some embodiments, the energy dissipation rate is calculated based on the reactor structural parameters, system physical property parameters, and operating parameters, including calculating the energy dissipation rate according to the following formula:

[0008]

[0009] Where ε represents the energy dissipation rate within the micro-interface generator, W / kg; λ represents the gas-liquid ratio within the micro-interface generator; ρ L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 V0 represents the volume of the micro-interface generator, in meters. 3 g represents the acceleration due to gravity, 9.81 m / s². 2 H0 represents the internal height of the slurry-bed heavy oil hydrotreating reactor, in meters (m); S0 represents the cross-sectional area of ​​the slurry-bed heavy oil hydrotreating reactor, in square meters (m²). 2 S1 represents the cross-sectional area of ​​the micro-interface generator outlet, in m³. 2 ;P m Q represents the operating pressure, Pa; ΔP represents the pressure difference between the inside and outside of the micro-interface generator, Pa; L0 The volumetric flow rate of fresh heavy oil in a slurry bed heavy oil hydrotreating reactor is expressed in m³. 3 / s.

[0010] In some embodiments, calculating the bubble size based on the energy dissipation rate includes calculating the bubble size according to the following formula:

[0011]

[0012] d max =0.75(σ L / ρ L ) 0.6 ε -0.4

[0013] d min =11.4(μ) L / ρ L ) 0.75 ε -0.25

[0014] Where, d 32 The diameter of the bubbles in a slurry bed heavy oil micro-interface hydroenhanced reactor is expressed in meters (m). max d min σ represents the maximum and minimum bubble diameters within the micro-interface generator, in meters (m); L The interfacial tension of the gas-liquid interface in a slurry bed heavy oil hydrogenation system is expressed in N / m; ρ L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 μ L ε represents the dynamic viscosity of the liquid phase in the slurry bed heavy oil hydrogenation system, Pa·s; ε represents the energy dissipation rate in the micro-interface generator, W / kg.

[0015] In some embodiments, calculating the rising velocity of a single bubble in an infinitely large static liquid phase based on the bubble size includes calculating the rising velocity of a single bubble in an infinitely large static liquid phase according to the following formula:

[0016]

[0017] Mo = gμ L 4 / ρ L σ L 3

[0018] d e '=d 32 (ρ L g / σ L ) 1 / 2

[0019] Where v0 represents the rising velocity of a single bubble in an infinitely large, static liquid phase, in m / s; and g represents the acceleration due to gravity, 9.81 m / s². 2 μ L The ρ represents the liquid phase dynamic viscosity of the slurry bed heavy oil hydrotreating system, in Pa·s. L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 ;σ L The d represents the interfacial tension between gas and liquid in a slurry bed heavy oil hydrogenation system, in N / m. 32 The K value represents the bubble diameter in a slurry bed heavy oil micro-interface hydroenhanced reactor, in meters (m). b c and n represent empirical constants.

[0020] In some embodiments, the hydrogen transport capacity of the slurry bed heavy oil micro-interface enhancement reaction is calculated based on the average rising velocity of microbubbles and the bubble size in the micro-interface system, including calculating the average rising velocity of microbubbles in the micro-interface system according to the following formula:

[0021]

[0022] v G =Q G / S0

[0023] v L =Q L / S0

[0024] Among them, v 32 v0 represents the average rising velocity of microbubbles in the micro-interface system, in m / s; v0 represents the rising velocity of a single bubble in an infinitely large, still liquid, in m / s; v0 G V represents apparent gas velocity, m / s; L Q represents the apparent liquid velocity, in m / s; GThe volumetric flow rate of hydrogen at the inlet of a slurry-bed heavy oil hydrotreating reactor, expressed in m³. 3 / s;Q L The volumetric flow rate of heavy oil at the inlet of the slurry bed heavy oil hydrotreating reactor, in m³. 3 / s.

[0025] In some embodiments, the hydrogen transport capacity of the slurry bed heavy oil micro-interface enhancement reaction is calculated based on the average rising velocity and bubble size of the microbubbles in the micro-interface system, including calculating the hydrogen transport capacity of the slurry bed heavy oil micro-interface enhancement reaction according to the following formula:

[0026]

[0027] Where, N T The amount of hydrogen transported in mol represents the micro-interface enhancement reaction of slurry-bed heavy oil; P m Q represents operating pressure, Pa; G This represents the actual flow rate of gas within the MIG, in meters. 3 / s;H A The Henry's law representing the concentration of hydrogen in heavy oil, expressed in Pa·m. 3 / mol; v 32 The value d represents the average rising velocity of microbubbles in the micro-interface system, in m / s. 32 H0 represents the bubble diameter in the slurry-bed heavy oil micro-interface hydroenhanced reactor (m); H0 represents the internal height of the slurry-bed heavy oil hydroenhanced reactor (m); S0 represents the cross-sectional area of ​​the slurry-bed heavy oil hydroenhanced reactor (m²). 2 ; x represents the mole fraction of hydrogen in heavy oil; ρ L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 M1 represents the average molar mass of heavy oil, in kg / mol.

[0028] In some embodiments, the method further includes: determining, when the target design parameters of the slurry-bed heavy oil hydrotreating micro-interface reactor are taken at different values, the influence of operating pressure on at least one of the following parameters under each value: bubble size of the heavy oil hydrotreating system, gas-liquid interfacial area of ​​the heavy oil hydrotreating system, liquid-side mass transfer coefficient of the heavy oil hydrotreating system, liquid-side volumetric mass transfer coefficient of the heavy oil hydrotreating system, residence time of heavy oil in the reactor of the heavy oil hydrotreating system, hydrogen transport rate based on interfacial hydrogen transport mechanism, hydrogen transport rate based on pressure hydrogen transport mechanism, and the relative magnitude of interfacial hydrogen transport rate and pressure hydrogen transport rate of the heavy oil hydrotreating system; and determining the value of the target design parameters of the slurry-bed heavy oil hydrotreating micro-interface reactor based on the influence law.

[0029] The second aspect of this specification provides a device for determining the hydrogen transport capacity of a slurry-bed heavy oil micro-interface enhanced reaction, comprising: an acquisition unit for acquiring reactor structural parameters, system physical property parameters, and operating parameters of the slurry-bed heavy oil micro-interface enhanced reaction; a first calculation unit for calculating the energy dissipation rate based on the reactor structural parameters, system physical property parameters, and operating parameters; a second calculation unit for calculating the bubble size based on the energy dissipation rate; a third calculation unit for calculating the rising velocity of a single bubble in an infinitely large static liquid phase based on the bubble size; a fourth calculation unit for calculating the average rising velocity of microbubbles in the micro-interface system based on the rising velocity of a single bubble in the infinitely large static liquid phase; and a fifth calculation unit for calculating the hydrogen transport capacity of the slurry-bed heavy oil micro-interface enhanced reaction based on the average rising velocity of microbubbles in the micro-interface system and the bubble size.

[0030] In some embodiments, the first computing unit 20 calculates the energy dissipation rate according to the following formula:

[0031]

[0032] Where ε represents the energy dissipation rate within the micro-interface generator, W / kg; λ represents the gas-liquid ratio within the micro-interface generator; ρ L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 V0 represents the volume of the micro-interface generator, in meters. 3 g represents the acceleration due to gravity, 9.81 m / s². 2 H0 represents the internal height of the slurry-bed heavy oil hydrotreating reactor, in meters (m); S0 represents the cross-sectional area of ​​the slurry-bed heavy oil hydrotreating reactor, in square meters (m²). 2 S1 represents the cross-sectional area of ​​the micro-interface generator outlet, in m³. 2 ;P m Q represents the operating pressure, Pa; ΔP represents the pressure difference between the inside and outside of the micro-interface generator, Pa; L0 The volumetric flow rate of fresh heavy oil in a slurry bed heavy oil hydrotreating reactor is expressed in m³. 3 / s.

[0033] In some embodiments, the second calculation unit 30 calculates the bubble size according to the following formula:

[0034]

[0035] d max =0.75(σ L / ρ L ) 0.6 ε -0.4

[0036] d min =11.4(μ) L / ρL ) 0.75 ε -0.25

[0037] Where, d 32 The diameter of the bubbles in a slurry bed heavy oil micro-interface hydroenhanced reactor is expressed in meters (m). max d min σ represents the maximum and minimum bubble diameters within the micro-interface generator, in meters (m); L The interfacial tension of the gas-liquid interface in a slurry bed heavy oil hydrogenation system is expressed in N / m; ρ L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 μ L ε represents the dynamic viscosity of the liquid phase in the slurry bed heavy oil hydrogenation system, Pa·s; ε represents the energy dissipation rate in the micro-interface generator, W / kg.

[0038] In some embodiments, the third calculation unit 40 calculates the rising velocity of a single bubble in an infinitely large static liquid phase according to the following formula:

[0039]

[0040] Mo = gμ L 4 / ρ L σ L 3

[0041] d e '=d 32 (ρ L g / σ L ) 1 / 2

[0042] Where v0 represents the rising velocity of a single bubble in an infinitely large, static liquid phase, in m / s; and g represents the acceleration due to gravity, 9.81 m / s². 2 μ L The ρ represents the liquid phase dynamic viscosity of the slurry bed heavy oil hydrotreating system, in Pa·s. L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 ;σ L The d represents the interfacial tension between gas and liquid in a slurry bed heavy oil hydrogenation system, in N / m. 32 The K value represents the bubble diameter in a slurry bed heavy oil micro-interface hydroenhanced reactor, in meters (m). b c and n represent empirical constants.

[0043] In some embodiments, the fourth calculation unit 50 calculates the average rising velocity of microbubbles in the micro-interface system according to the following formula:

[0044]

[0045] v G =Q G / S0

[0046] v L =Q L / S0

[0047] Among them, v 32 v0 represents the average rising velocity of microbubbles in the micro-interface system, in m / s; v0 represents the rising velocity of a single bubble in an infinitely large, still liquid, in m / s; v0 G V represents apparent gas velocity, m / s; L Q represents the apparent liquid velocity, in m / s; G The volumetric flow rate of hydrogen at the inlet of a slurry-bed heavy oil hydrotreating reactor, expressed in m³. 3 / s;Q L The volumetric flow rate of heavy oil at the inlet of the slurry bed heavy oil hydrotreating reactor, in m³. 3 / s.

[0048] In some embodiments, the fifth calculation unit 60 calculates the hydrogen transport amount for the slurry bed heavy oil micro-interface enhancement reaction according to the following formula:

[0049]

[0050] Where, N T The amount of hydrogen transported in mol represents the micro-interface enhancement reaction of slurry-bed heavy oil; P m Q represents operating pressure, Pa; G This represents the actual flow rate of gas within the MIG, in meters. 3 / s;H A The Henry's law representing the concentration of hydrogen in heavy oil, expressed in Pa·m. 3 / mol; v 32 The value d represents the average rising velocity of microbubbles in the micro-interface system, in m / s. 32 H0 represents the bubble diameter in the slurry-bed heavy oil micro-interface hydroenhanced reactor (m); H0 represents the internal height of the slurry-bed heavy oil hydroenhanced reactor (m); S0 represents the cross-sectional area of ​​the slurry-bed heavy oil hydroenhanced reactor (m²). 2 ; x represents the mole fraction of hydrogen in heavy oil; ρ L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 M1 represents the average molar mass of heavy oil, in kg / mol.

[0051] In some embodiments, the apparatus further includes: a first determining unit, configured to determine, when the target design parameters of the slurry-bed heavy oil hydrotreating micro-interface reactor are of different values, the influence of operating pressure on at least one of the following parameters under each of the following values: bubble size of the heavy oil hydrotreating system, gas-liquid interfacial area of ​​the heavy oil hydrotreating system, liquid-side mass transfer coefficient of the heavy oil hydrotreating system, liquid-side volumetric mass transfer coefficient of the heavy oil hydrotreating system, residence time of heavy oil in the reactor of the heavy oil hydrotreating system, hydrogen transport rate based on interfacial hydrogen transport mechanism, hydrogen transport rate based on pressure hydrogen transport mechanism, and the relative magnitude of interfacial hydrogen transport rate and pressure hydrogen transport rate of the heavy oil hydrotreating system; and a second determining unit, configured to determine the values ​​of the target design parameters of the slurry-bed heavy oil hydrotreating micro-interface reactor based on the influence characteristics.

[0052] A third aspect of this specification provides an electronic device, comprising: a memory and a processor, wherein the processor and the memory are communicatively connected to each other, the memory stores computer instructions, and the processor executes the computer instructions to implement the method for determining the hydrogen transport amount in the micro-interface enhancement reaction of slurry bed heavy oil as described in any one of the first aspects.

[0053] This manual provides a method, apparatus, and electronic equipment for determining hydrogen transport in a slurry-bed heavy oil micro-interface enhanced reaction. It innovatively establishes a physical model for a slurry-bed heavy oil hydrotreating micro-interface reactor micro-interface unit applicable to both purely pneumatic and purely hydraulic or gas-liquid combined operation conditions. Based on this physical model, a mathematical model for the energy dissipation rate is derived, which can then be used to further calculate the bubble size d. 32 The average rising velocity v of microbubbles in the micro-interface system 32 The hydrogen transfer rate is then calculated. This method is applicable to both purely pneumatic and purely hydraulic or gas-liquid combined operating conditions, making it widely applicable and suitable for guiding the design of slurry-bed heavy oil hydrogenation micro-interface reactors and reaction system design. Attached Figure Description

[0054] To more clearly illustrate the technical solutions in the embodiments of this application or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments recorded in this application. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0055] Figure 1 A simplified physical model diagram of the micro-interface formation process within the MIG;

[0056] Figure 2This is a graph showing the relationship between the actual ventilation rate and the actual gas-liquid ratio within the MIG.

[0057] Figure 3 This is a schematic diagram of the method for determining the hydrogen transport capacity of the micro-interface enhancement reaction of slurry bed heavy oil provided in this specification.

[0058] Figure 4 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the bubble d of the system. 32 The effect of size;

[0059] Figure 5 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the gas-liquid interphase area a of the system;

[0060] Figure 6 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the liquid-side mass transfer coefficient k. L The impact;

[0061] Figure 7 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the liquid-side volumetric mass transfer coefficient k. L The impact of a;

[0062] Figure 8 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the residence time t of the heavy oil in the reactor. e The impact;

[0063] Figure 9 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the interfacial hydrogen transport capacity Na.

[0064] Figure 10 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the system's pressure-driven hydrogen delivery rate Np;

[0065] Figure 11 This reflects the influence of the operating pressure Pm of the MIR heavy oil hydrotreating system on the relative magnitudes of the interfacial hydrogen transport capacity Na and the pressure hydrogen transport capacity Np.

[0066] Figure 12 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the bubble d of the system. 32 The effect of size;

[0067] Figure 13 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the gas-liquid interphase area a of the system;

[0068] Figure 14 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the liquid-side mass transfer coefficient k. L The impact;

[0069] Figure 15 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the liquid-side volumetric mass transfer coefficient k. L The impact of a;

[0070] Figure 16 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the residence time t of the heavy oil in the reactor. e The impact;

[0071] Figure 17 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the interfacial hydrogen transport capacity Na.

[0072] Figure 18 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the system's pressure-driven hydrogen delivery rate Np;

[0073] Figure 19 This reflects the influence of the operating pressure Pm of the MIR heavy oil hydrotreating system on the relative magnitudes of the interfacial hydrogen transport capacity Na and the pressure hydrogen transport capacity Np.

[0074] Figure 20 This is a schematic diagram of the apparatus for determining the hydrogen transport capacity of the slurry bed heavy oil micro-interface enhancement reaction provided in this specification.

[0075] Figure 21 A schematic diagram of the electronic device provided in this specification is shown. Detailed Implementation

[0076] To enable those skilled in the art to better understand the technical solutions in this application, the technical solutions in the embodiments of this application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only a part of the embodiments of this application, and not all of the embodiments. Based on the embodiments in this application, all other embodiments obtained by those skilled in the art without creative effort should fall within the scope of protection of this application.

[0077] The purpose of this invention is to provide a mathematical model for hydrogen transport in a slurry bed heavy oil hydrotreating micro-interface reactor that is applicable to both purely pneumatic and purely hydraulic or gas-liquid combined operating conditions. This model is intended to study the influence of reactor structure, system properties, and operating parameters on hydrogen transport, thereby providing guidance for the design of slurry bed heavy oil hydrotreating micro-interface reactors and the design of their reaction systems.

[0078] The following section details the derivation of the mathematical model for hydrogen transport in a slurry-bed heavy oil hydrotreating micro-interface reactor, which is applicable to both purely pneumatic and purely hydraulic or gas-liquid combined operation conditions.

[0079] 1. Analyze the parameters affecting hydrogen transport in the slurry bed heavy oil micro-interface hydrogenation reaction system.

[0080] The macroscopic reaction rate and feed conversion rate of the heavy oil hydrotreating system are determined by the total hydrogen molecule transport (NT) in the liquid phase of the system. The mass transfer of hydrogen within the reactor is determined based on two mechanisms: pressure transport and interfacial transport.

[0081] N T =N a +N p (1)

[0082] Where N a The hydrogen transport rate based on the interface hydrogen transport mechanism is expressed in mol; N. p The hydrogen transport rate is expressed in mol based on the pressure-based hydrogen transport mechanism.

[0083] 2. Obtain the hydrogen transport capacity N based on the interface hydrogen transport mechanism. a

[0084] Assuming the hydrogen bubbles in the system are of uniform size and the hydrogen transport rate across the gas-liquid interface is... Similarly, the hydrogen transport capacity N based on the interface hydrogen transport mechanism... a The total number of stable bubbles in the system, n0 (number of bubbles), and the average residence time t of heavy oil in the reactor e (s) are jointly determined, as shown in equation (2):

[0085]

[0086] Analysis of the movement process of heavy oil in the reactor, the average residence time t of heavy oil in the reactor. e It can be represented as:

[0087]

[0088] Among them, V L Let m be the volume of heavy oil in the reactor. 3 Q L The volumetric flow rate of fresh heavy oil entering the reactor is m 3 / s.

[0089] V L Determined by the relative motion between the hydrogen and heavy oil phases, analysis of the gas-liquid two-phase motion yields the following:

[0090]

[0091] Where H0 is the height of the reactor cavity, in meters (m); and S0 is the cross-sectional area of ​​the reactor, in meters (m²).2 ;v 32 denoted as the average rising velocity of bubbles within the reactor, in m / s.

[0092] Substituting equation (4) into equation (3), we get:

[0093]

[0094] The total number of stable bubbles in the system, n0, is obtained from the conservation of gas volume and analysis of bubble motion, i.e.:

[0095]

[0096] Q G The volumetric flow rate of hydrogen is m. 3 / s;d 32 Let be the average diameter of the Sauter bubbles in the reactor, in meters (m).

[0097] Hydrogen transport rate at the gas-liquid interface Based on Fick's Law, that is:

[0098]

[0099] J z＝0 The mass flux of hydrogen at the gas-liquid interface of the gas bubble is expressed in mol / m³. 2 ;D L Let m be the liquid-phase diffusion coefficient of hydrogen in heavy oil. 2 / s; t is any time (s) during which the heavy oil resides in the reactor; C H * (mol / m 3 ) represents the saturated hydrogen concentration at the gas-liquid interface, calculated using Henry's Law as shown in equation (8):

[0100]

[0101] Where P m Operating pressure, Pa; H A Here is the Henry coefficient, Pa·m 3 / mol.

[0102] Substituting equations (5) to (8) into equation (2), we get:

[0103]

[0104] 3. Obtain the hydrogen transport volume N based on the pressure hydrogen transport mechanism. P

[0105] Hydrogen transport capacity N based on pressure transport mechanism PBoth its limiting value and its limit value are determined by Henry's law, and are also subject to the bulk volume V of the heavy oil liquid phase. L Operating pressure P m and the average residence time t of heavy oil e Impact. Assume N P The limit of hydrogen solubility in the system is:

[0106] N p =V L ×C H * (10)

[0107] When the molar mass of heavy oil is M1 (kg / mol), C H *It has the following relationship with the mole fraction of hydrogen in heavy oil, x:

[0108]

[0109] Where ρL is the density of heavy oil, kg / m³ 3 .

[0110] From equations (4), (9), and (11), we get:

[0111]

[0112] 4. Obtain the total amount of hydrogen molecules transported.

[0113] From equations (1)(9)(12), we get:

[0114]

[0115] In equation (13), the average rising velocity v of the microbubbles in the micro-interface system is... 32 The structure-activity regulation mathematical model has been introduced in the prior art, and its expression is equation (14):

[0116]

[0117] In equation (14), v G (m / s) and v L (m / s) represent the apparent gas velocity and apparent liquid velocity, respectively, and are calculated according to the following equations (15) and (16):

[0118] v G =Q G / S0 (15)

[0119] v L =Q L / S0 (16)

[0120] In equation (14), v0 (m / s) is the rising velocity of a single bubble in an infinitely large static liquid phase, which can be calculated according to the following empirical equation (17):

[0121]

[0122] In equation (17):

[0123] Mo = gμ L 4 / ρ L σ L 3 (18)

[0124] d e '=d 32 (ρ L g / σ L ) 1 / 2 (19)

[0125] 5. Establishing a slurry-bed heavy oil micro-interface hydrogenation enhanced reactor with bubble size d 32 General Mathematical Model

[0126] Slurry bed heavy oil micro-interface hydroenhanced reactor bubble size d 32 The general mathematical model has been introduced in the prior art, and its expression is shown in equation (20):

[0127]

[0128] In equation (20):

[0129] d max =0.75(σ L / ρ L ) 0.6 ε -0.4 (twenty one)

[0130] d min =11.4(μ) L / ρ L ) 0.75 ε -0.25 (twenty two)

[0131] In equations (21) and (22), ε (W / kg) is the energy dissipation rate of the micro-interface unit.

[0132] 6. Establish a mathematical model for the energy dissipation rate of the micro-interface unit (MIG) in a slurry bed heavy oil micro-interface hydroenhanced reactor.

[0133] Figure 1 This is a simplified physical model diagram of the micro-interface formation process within the MIG. The rectangular region represents the interior of the cavity of the micro-interface generator (MIG), and Q... L0This indicates the flow rate of the liquid entering the MIG chamber; the flow rate of the liquid entering the MIG chamber is the same as the flow rate of the liquid exiting the MIG chamber; Q G Q represents the flow rate of gas entering the MIG chamber; L1 This indicates the flow rate of the circulating fluid re-entering the MIG chamber from the outlet; D1 represents the diameter of the cylindrical MIG chamber; P m This indicates the operating pressure of the micro-interface enhanced reactor (MIR). 0-0 indicates the MIG inlet position, and 1-1 indicates the MIG outlet position.

[0134] based on Figure 1 The physical model shown illustrates the following physical processes occurring within the MIG:

[0135] Before the gas was introduced, the MIG was filled with a static reaction liquid. When the gas was introduced, due to the initial gas pressure P... G0 (Pa) and system operating pressure P m There is a pressure difference ΔP(Pa) between the gas and liquid phases. The gas transfers some of its static pressure energy to the liquid, causing turbulence and breaking the continuous gas phase into a dispersed bubble phase. The gas pressure itself rapidly decreases to the operating pressure within the micro-interface enhanced reactor (MIR). The resulting homogeneous gas-liquid mixture flows out of the MIG, with some liquid entering the MIG via internal circulation along with fresh liquid, serving as a medium for releasing the gas's static pressure energy. The energy required for the entire system to operate is almost entirely provided by gas pressure energy.

[0136] The above process can be analyzed from an energy perspective. During the process of a high-pressure gas entering the MIG and releasing its pressure energy, the system's energy is transferred and converted through gas-liquid interactions. The pressure energy released by the gas is converted into the kinetic energy of the liquid, the gas-liquid interface energy, and the internal energy dissipated due to friction.

[0137] To establish a mathematical model for the liquid energy dissipation rate ε within the MIG, this specification takes the gas-liquid two-phase system entering and exiting the MIG as the research object and makes the following assumptions:

[0138] ① The MIR operates in a continuous steady-state state;

[0139] ②The gas-liquid mixing process inside the MIG is adiabatic and isothermal;

[0140] ③ The gas decompression process is completed in a very short time, and the pressure inside the MIG is the operating pressure;

[0141] ④ Neglect the changes in gas kinetic energy and gravitational potential energy between the gas and liquid phases;

[0142] ⑤ The gas is a single-component ideal gas.

[0143] When the MIR is operating in steady state, for the gas-liquid two-phase system entering and exiting the MIG, since no external force does work and the process is adiabatic and isothermal, the following energy conservation relationship holds:

[0144] 0 = ΔE L +ΔE G +ρ L V L ε (23)

[0145] In equation (23), ΔE L and ΔE G The mechanical energy changes, W and V, represent the changes in mechanical energy during the entry and exit of liquid and gas into and from the MIG, respectively. L Let m be the volume of the liquid inside the MIG. 3 ;ρ L V L ε represents the energy dissipated by the liquid within the MIG, including internal energy and bubble surface energy. From equation (23), we can obtain:

[0146]

[0147] To derive the mathematical expression for ε, it is necessary to modify ΔE in equation (24). L ΔE G and V L The calculation expressions for the three key parameters are established respectively.

[0148] I. Change in fluid mechanical energy ΔE when entering and exiting the MIG L

[0149] When the MIR is operating in steady state, two fluids enter the MIG: fresh fluid (flow rate Q). L0 m 3 / s) and circulating liquid (flow rate Q) L1 m 3 / s). For circulating fluids, since they have already acquired a certain amount of energy within the MIG, their energy density can be considered constant before and after entering and exiting the MIG. Therefore, when the changes in hydrostatic energy and gravitational potential energy are negligible, the change in the mechanical energy of the fluid entering and exiting the MIG only considers the change in the kinetic energy of the fresh fluid. In the above... Figure 1 Under the condition, Q L0 Since its initial kinetic energy is relatively small, it can be ignored. Therefore, the change in mechanical energy during the process of fresh liquid entering and exiting the MIG can be expressed as:

[0150]

[0151] The term in parentheses on the right side of equation (25) represents the average outflow velocity of the gas-liquid mixture at the MIG outlet. Where S1 is the cross-sectional area of ​​the MIG outlet, in meters... 2 Q G The actual flow rate of the gas inside the MIG, m3 / s. Let the actual gas-liquid ratio in the MIG be λ, i.e.:

[0152]

[0153] Thus, equation (25) can be simplified to equation (27):

[0154]

[0155] When the reactor operates at a steady state, the liquid in its main body is forced to flow out of the reactor due to the introduction of gas. Therefore, the flow rate of the liquid flowing out of the reactor can be approximately equal to the actual gas flow rate. According to the conservation of energy, the circulating liquid flow rate Q L1 can be obtained through mathematical derivation:

[0156]

[0157] In equation (28), S0 (m 2 ) and H0 (m) are the cross-sectional area and the inner cavity height of the reactor respectively. By联立 equations (26) and (28), the actual gas-liquid ratio λ in the MIG can be calculated according to equation (29)

[0158]

[0159] When λ is constant, from equation (29), we can get:

[0160]

[0161] Since the value inside the square root must be no less than 0, equation (30) should satisfy the condition:

[0162] λ < S0 / S1 or S1 < S0 / λ (31)

[0163] Inequality (31) indicates that when the cross-sectional area of the reactor is constant, to maintain a large gas-liquid ratio in the MIG, there is an upper limit value for the cross-sectional area of the MIG; when the structure of the reactor is constant, if the required gas-liquid ratio in the MIG is larger, the actual gas flow rate in the MIG should also be larger, and vice versa. Figure 2 It is a relationship diagram of the actual gas flow rate and the actual gas-liquid ratio in the MIG.

[0164] From Figure 2 it can be seen that the actual gas-liquid ratio in the MIG increases with the increase of the gas flow rate, but when the gas flow rate increases to a certain value, the influence of the gas flow rate on the gas-liquid ratio is small. After substituting equation (30) into equation (27), we can get:

[0165]

[0166] Equation (32) is the mathematical model for the change in the mechanical energy of the liquid entering and exiting the MIG. The relationship between the actual gas-liquid ratio λ inside the MIG and the gas-liquid ratio λ0 before entering the MIG should be clearly defined to facilitate the control of actual operating conditions.

[0167] Since the gas is an ideal gas, the gas flow rate Q before entering the MIG is... G0 (m 3 / s) and the actual gas flow rate Q inside the MIG G The following relationship exists between them:

[0168]

[0169] Substituting equation (33) into equation (30), we get:

[0170]

[0171] Therefore, λ0 and λ have the following relationship:

[0172]

[0173] or,

[0174]

[0175] II. Changes in the mechanical energy of gases entering and exiting the MIG

[0176] Because of the low gas density, only the change in gas static pressure energy is considered during the process of gas entering the MIG and forming microbubbles. Let the initial gas flow rate and pressure entering the MIG be Q, respectively. G0 (m 3 / s) and P G0 (Pa), then the change in mechanical energy ΔE during the gas entering and exiting the MIG. G for

[0177] ΔE G =P G0 Q G0 ln(P m / P G0 (37)

[0178] because

[0179] P G0 =P m +ΔP (38)

[0180] therefore

[0181]

[0182] The following sections of this paper will explore the effect of operating pressure under a fixed gas-liquid ratio, but P mIt affects the actual intake airflow within the MIG, namely:

[0183]

[0184] In equation (40), Q G * (m 3 / s) and P G * (1.01×10 5 Pa) represents the gas flow rate and supply pressure under standard conditions, respectively, and their values ​​are generally constant. To ensure that the actual gas-liquid ratio remains constant under changing operating pressure, let...

[0185] (When the gas-liquid ratio λ is constant, k) m (41) (a constant)

[0186] Since the gas is an ideal gas, the actual gas flow rate Q in the reactor is... G for:

[0187]

[0188] From equations (41) and (42), we can obtain:

[0189]

[0190] From equations (34) and (43), we can obtain:

[0191]

[0192] Equation (44) shows that when the operating pressure P m When the required gas-liquid ratio λ is constant, k m It is certain. In other words, if P is changed... m When λ needs to be maintained at a constant value, the actual gas supply flow rate Q G0 Adjustments can be made according to equation (34). Combining equations (39), (41), and (44), we can obtain:

[0193]

[0194] Equation (45) is the expression for the change in mechanical energy of the gas inside the MIG. As can be seen from equation (45), the magnitude of the static pressure energy released by the gas is related to the initial gas pressure, operating pressure, actual gas-liquid ratio, and reactor structure.

[0195] III. Liquid volume inside the MIG

[0196] When the MIG volume V0(m 3 At a given time, V L and its liquid content φL Relevant, namely:

[0197] V L =V0φ L (46)

[0198] φ L Determined by the gas-liquid ratio λ within the MIG, i.e.:

[0199]

[0200] From equations (46) and (47), we can obtain:

[0201]

[0202] Equation (48) is the formula for calculating the liquid volume inside the MIG. Among them, λ can be calculated by equation (36).

[0203] To maximize the release of the pressure energy released by the gas and break it into micron-sized bubbles, a certain amount of liquid is required as a medium. Equation (48) shows that the larger the gas-liquid ratio in the MIG, the smaller the actual amount of liquid in the MIG. Therefore, in order to ensure that there is an appropriate amount of liquid in the MIG for the maximum release of gas pressure energy, the actual gas-liquid ratio in the MIG should not be too large.

[0204] Substituting equations (32), (45), and (48) into equation (24), we get:

[0205]

[0206] Based on the above analysis, this specification provides a method for determining the hydrogen transport capacity in a slurry-bed heavy oil micro-interface enhancement reaction. For example... Figure 3 As shown, the method includes the following steps:

[0207] S10: Obtain reactor structural parameters, system physical property parameters, and operating parameters for the slurry bed heavy oil micro-interface enhancement reaction.

[0208] The reactor structural parameters include at least one of the following: the volume V0 of the micro-interface generator, the height H0 of the inner cavity of the slurry bed heavy oil hydrogenation reactor, the cross-sectional area S0 of the slurry bed heavy oil hydrogenation reactor, and the cross-sectional area S1 of the outlet of the micro-interface generator.

[0209] The system physical properties include at least one of the following: liquid phase density of the slurry bed heavy oil hydrogenation system, gas-liquid interfacial tension of the slurry bed heavy oil hydrogenation system, and liquid phase dynamic viscosity of the slurry bed heavy oil hydrogenation system.

[0210] Operating parameters include at least one of the following: operating pressure P m The pressure difference ΔP between the inside and outside of the micro-interface generator, and the volumetric flow rate Q of fresh heavy oil in the slurry bed heavy oil hydrotreating reactor.L0 The gas-liquid ratio λ inside the micro-interface generator.

[0211] S20: Calculate the energy dissipation rate based on the reactor structural parameters, system physical property parameters, and operating parameters.

[0212] Specifically, the energy dissipation rate can be calculated according to the above formula (49).

[0213] In formula (49), ε represents the energy dissipation rate within the micro-interface generator, W / kg; λ represents the gas-liquid ratio within the micro-interface generator; ρ L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 V0 represents the volume of the micro-interface generator, in meters. 3 g represents the acceleration due to gravity, 9.81 m / s². 2 H0 represents the internal height of the slurry-bed heavy oil hydrotreating reactor, in meters (m); S0 represents the cross-sectional area of ​​the slurry-bed heavy oil hydrotreating reactor, in square meters (m²). 2 S1 represents the cross-sectional area of ​​the micro-interface generator outlet, in m³. 2 ;P m Q represents the operating pressure, Pa; ΔP represents the pressure difference between the inside and outside of the micro-interface generator, Pa; L0 The volumetric flow rate of fresh heavy oil in a slurry bed heavy oil hydrotreating reactor is expressed in m³. 3 / s.

[0214] S30: Calculate the bubble size based on the energy dissipation rate.

[0215] Specifically, the bubble size can be calculated using the formulas (20), (21) and (22) above.

[0216] In formulas (20)-(22), d 32 The diameter of the bubbles in a slurry bed heavy oil micro-interface hydroenhanced reactor is expressed in meters (m). max d min σ represents the maximum and minimum bubble diameters within the micro-interface generator, in meters (m); L The interfacial tension of the gas-liquid interface in a slurry bed heavy oil hydrogenation system is expressed in N / m; ρ L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 μ L ε represents the dynamic viscosity of the liquid phase in the slurry bed heavy oil hydrogenation system, Pa·s; ε represents the energy dissipation rate in the micro-interface generator, W / kg.

[0217] S40: Calculate the rising velocity of a single bubble in an infinitely large static liquid phase based on the bubble size.

[0218] Specifically, the rising velocity of a single bubble in an infinitely large static liquid phase can be calculated using the formulas (17)-(19) above.

[0219] In formulas (17)-(19), v0 represents the rising velocity of a single bubble in an infinitely large static liquid phase, m / s; g represents the acceleration due to gravity, 9.81 m / s². 2 μ L The ρ represents the liquid phase dynamic viscosity of the slurry bed heavy oil hydrotreating system, in Pa·s. L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 ;σ L The d represents the interfacial tension between gas and liquid in a slurry bed heavy oil hydrogenation system, in N / m. 32 The K value represents the bubble diameter in a slurry bed heavy oil micro-interface hydroenhanced reactor, in meters (m). b c and n represent empirical constants. For heavy oil hydrogenation systems, c can take a value of 1.2 and n can take a value of 1.4.

[0220] S50: Calculate the average rising velocity of microbubbles in the micro-interface system based on the rising velocity of a single bubble in an infinitely large static liquid phase.

[0221] Specifically, the average rising velocity of microbubbles in the micro-interface system can be calculated according to the above formulas (14)-(16).

[0222] In formulas (14)-(16), v 32 v0 represents the average rising velocity of microbubbles in the micro-interface system, in m / s; v0 represents the rising velocity of a single bubble in an infinitely large, still liquid, in m / s; v0 G V represents apparent gas velocity, m / s; L Q represents the apparent liquid velocity, in m / s; G The volumetric flow rate of hydrogen at the inlet of a slurry-bed heavy oil hydrotreating reactor, expressed in m³. 3 / s;Q L The volumetric flow rate of heavy oil at the inlet of the slurry bed heavy oil hydrotreating reactor, in m³. 3 / s.

[0223] S60: Calculate the hydrogen transport capacity of the micro-interface enhancement reaction in slurry bed heavy oil based on the average rising velocity and bubble size of the microbubbles in the micro-interface system.

[0224] Specifically, the amount of hydrogen transported by the micro-interface enhancement reaction of slurry bed heavy oil can be calculated according to the above formula (13).

[0225] In formula (13), N T The amount of hydrogen transported in mol represents the micro-interface enhancement reaction of slurry-bed heavy oil; P m Q represents operating pressure, Pa; G This represents the actual flow rate of gas within the MIG, in meters. 3 / s;H AThe Henry's law representing the concentration of hydrogen in heavy oil, expressed in Pa·m. 3 / mol; v 32 The value d represents the average rising velocity of microbubbles in the micro-interface system, in m / s. 32 H0 represents the bubble diameter in the slurry-bed heavy oil micro-interface hydroenhanced reactor (m); H0 represents the internal height of the slurry-bed heavy oil hydroenhanced reactor (m); S0 represents the cross-sectional area of ​​the slurry-bed heavy oil hydroenhanced reactor (m²). 2 ; x represents the mole fraction of hydrogen in heavy oil; ρ L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 M1 represents the average molar mass of heavy oil, in kg / mol.

[0226] The method for determining hydrogen transport in slurry-bed heavy oil micro-interface enhanced reactions provided in this manual innovatively establishes a physical model for a slurry-bed heavy oil hydrotreating micro-interface reactor micro-interface unit applicable to both purely pneumatic and purely hydraulic or gas-liquid combined operation conditions. Based on this physical model, a mathematical model for the energy dissipation rate is derived, which in turn allows for the further calculation of the bubble size d. 32 The average rising velocity v of microbubbles in the micro-interface system 32 The hydrogen transfer rate is then calculated. This method is applicable to both purely pneumatic and purely hydraulic or gas-liquid combined operating conditions, making it widely applicable and suitable for guiding the design of slurry-bed heavy oil hydrogenation micro-interface reactors and reaction system design.

[0227] In some embodiments, the method for determining the hydrogen transport capacity of the slurry bed heavy oil micro-interface enhancement reaction provided in this specification further includes the following steps S70 and S80.

[0228] S70: When the target design parameters of the slurry bed heavy oil hydrotreating micro-interface reactor are taken at different values, determine the influence of operating pressure on at least one of the following parameters under each value: bubble size of the heavy oil hydrotreating system, gas-liquid interfacial area of ​​the heavy oil hydrotreating system, liquid-side mass transfer coefficient of the heavy oil hydrotreating system, liquid-side volumetric mass transfer coefficient of the heavy oil hydrotreating system, residence time of heavy oil in the reactor of the heavy oil hydrotreating system, hydrogen transport rate based on interfacial hydrogen transport mechanism, hydrogen transport rate based on pressure hydrogen transport mechanism, and the relative magnitude of interfacial hydrogen transport rate and pressure hydrogen transport rate of the heavy oil hydrotreating system.

[0229] S80: Determine the target design parameters for the slurry bed heavy oil hydrogenation micro-interface reactor based on the aforementioned influence laws.

[0230] The target design parameters mentioned above may include at least one of the following: reactor height, reactor cross-sectional area, heavy oil density, heavy oil molar mass, operating pressure, operating temperature, liquid hourly space velocity, and hydrogen-to-oil ratio.

[0231] The methods described in S70 and S80 above will be illustrated below with two examples.

[0232] Example 1

[0233] This study investigates the effects of specific MIR heavy oil hydrotreating reactor structure and operating conditions on the system's hydrogen mass transfer process parameters (bubble size, gas-liquid interface area, mass transfer coefficient, heavy oil residence time, etc.) and hydrogen transfer rate.

[0234] The influence of operating pressure on the following parameters is calculated based on the reactor design parameters: bubble size in the heavy oil hydrogenation system, gas-liquid interphase area in the heavy oil hydrogenation system, liquid-side mass transfer coefficient in the heavy oil hydrogenation system, liquid-side volumetric mass transfer coefficient in the heavy oil hydrogenation system, residence time of heavy oil in the reactor in the heavy oil hydrogenation system, hydrogen transport rate based on interfacial hydrogen transport mechanism, hydrogen transport rate based on pressure hydrogen transport mechanism, and the relative magnitude of interfacial hydrogen transport rate and pressure hydrogen transport rate in the heavy oil hydrogenation system.

[0235] Reactor design parameters: Reactor height H0 = 50.0 m; Reactor cross-sectional area S0 = 19.63 m² 2 The density ρ of heavy oil L =800kg / m 3 The molar mass of the heavy oil is M1 = 0.416 kg / mol; the operating pressure is P. m =2.0-18MPa; Operating temperature: 430℃; Liquid hourly space velocity: 0.15h -1 Hydrogen-to-oil ratio: 700.

[0236] The results are attached. Figures 4-10 As shown.

[0237] Figure 4 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the bubble d of the system. 32 The effect of size. (By...) Figure 4 It can be seen that, under the investigated operating conditions, the bubble d in the MIR heavy oil hydrotreating system 32 It increases as the operating pressure Pm decreases, and vice versa. When Pm is high (e.g., greater than 10 MPa), d 32 The effect of Pm is relatively small; when Pm is low (e.g., less than 3 MPa), d 32 It increases sharply as Pm decreases.

[0238] Figure 5This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the gas-liquid interphase area a. Figure 5 It can be seen that, under the working conditions under investigation, the gas-liquid interface area a shows a trend of first increasing and then decreasing as Pm decreases.

[0239] Figure 6 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the liquid-side mass transfer coefficient k. L The impact. By Figure 6 It can be seen that, under the investigated operating conditions, the liquid-side mass transfer coefficient k of the system is... L It decreases as Pm decreases.

[0240] Figure 7 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the liquid-side volumetric mass transfer coefficient k. L The influence of a. (By) Figure 7 It can be seen that, under the investigated operating conditions, the liquid-side volumetric mass transfer coefficient k of the system is... L a shows a trend of first increasing and then decreasing as Pm decreases. (Comparison) Figures 5-7 It can be seen that the above k L The variation trend of a with Pm is mainly dominated by the gas-liquid interface area a of the system.

[0241] Figure 8 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the residence time t of the heavy oil in the reactor. e The impact. By Figure 8 It can be seen that, under the investigated operating conditions, the residence time t of heavy oil in the reactor is... e The length decreases as Pm decreases.

[0242] Figure 9 This reflects the effect of the operating pressure Pm in the MIR heavy oil hydrotreating system on the interfacial hydrogen transport capacity of Na. Figure 9 It can be seen that, under the operating conditions under investigation, the interfacial hydrogen transport capacity Na decreases as Pm decreases, and vice versa.

[0243] Figure 10 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the system's pressure-driven hydrogen delivery rate Np. Figure 10 It can be seen that, under the operating conditions under investigation, the system pressure hydrogen transport capacity Np decreases as Pm decreases, and vice versa.

[0244] Figure 11 This reflects the influence of the operating pressure Pm of the MIR heavy oil hydrotreating system on the relative magnitudes of the interfacial hydrogen transport capacity Na and the pressure hydrogen transport capacity Np. Figure 11It can be seen that, under the investigated operating conditions, the Na / Np ratio first increases and then decreases with decreasing Pm, and Na is consistently much larger than Np. This implies that, for the MIR heavy oil hydrotreating system, the interfacial hydrogen transport mechanism is more dominant than the pressure hydrogen transport mechanism.

[0245] Example 2

[0246] This study investigates the effects of specific MIR heavy oil hydrotreating reactor structure and operating conditions on the system's hydrogen mass transfer process parameters (bubble size, gas-liquid interface area, mass transfer coefficient, heavy oil residence time, etc.) and hydrogen transfer rate.

[0247] The influence of operating pressure on the following parameters is calculated based on the reactor design parameters: bubble size in the heavy oil hydrogenation system, gas-liquid interphase area in the heavy oil hydrogenation system, liquid-side mass transfer coefficient in the heavy oil hydrogenation system, liquid-side volumetric mass transfer coefficient in the heavy oil hydrogenation system, residence time of heavy oil in the reactor in the heavy oil hydrogenation system, hydrogen transport rate based on interfacial hydrogen transport mechanism, hydrogen transport rate based on pressure hydrogen transport mechanism, and the relative magnitude of interfacial hydrogen transport rate and pressure hydrogen transport rate in the heavy oil hydrogenation system.

[0248] Reactor design parameters: Reactor height H0 = 50.0 m; Reactor cross-sectional area S0 = 19.63 m² 2 The density ρ of heavy oil L =800kg / m 3 The molar mass of the heavy oil is M1 = 0.416 kg / mol; the operating pressure is P. m =2.0-18MPa; Operating temperature: 430℃; Liquid hourly space velocity: 0.15h -1 Hydrogen-to-oil ratio: 700.

[0249] Reactor design parameters: Reactor height H0 = 4.0 m; Reactor cross-sectional area S0 = 0.1256 m² 2 The density ρ of heavy oil L =800kg / m 3 The molar mass of the heavy oil is M1 = 0.416 kg / mol; the operating pressure is P. m =2.0-18MPa; Operating temperature: 450℃; Liquid hourly space velocity: 0.15h -1 Hydrogen-to-oil ratio: 1000.

[0250] The results are attached. Figures 12-18 As shown.

[0251] Figure 12 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the bubble d of the system. 32 The effect of size. (By...) Figure 12 It can be seen that, under the investigated operating conditions, the bubble d in the MIR heavy oil hydrotreating system32 It increases slightly as the operating pressure Pm decreases.

[0252] Figure 13 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the gas-liquid interphase area a. Figure 13 It can be seen that, under the working conditions under investigation, the gas-liquid interface area a increases as Pm decreases.

[0253] Figure 14 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the liquid-side mass transfer coefficient k. L The impact. By Figure 14 It can be seen that, under the investigated operating conditions, the liquid-side mass transfer coefficient k of the system is... L It decreases as Pm decreases.

[0254] Figure 15 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the liquid-side volumetric mass transfer coefficient k. L The influence of a. (By) Figure 15 It can be seen that, under the investigated operating conditions, the liquid-side volumetric mass transfer coefficient k of the system is... L a increases as Pm decreases. (Comparison) Figures 13-15 It can be seen that the above k L The variation trend of a with Pm is mainly dominated by the gas-liquid interface area a of the system.

[0255] Figure 16 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the residence time t of the heavy oil in the reactor. e The impact. By Figure 16 It can be seen that, under the investigated operating conditions, the residence time t of heavy oil in the reactor is... e The length decreases as Pm decreases, and this trend is more pronounced when Pm is low (e.g., less than 3.0 MPa).

[0256] Figure 17 This reflects the effect of the operating pressure Pm in the MIR heavy oil hydrotreating system on the interfacial hydrogen transport capacity of Na. Figure 17 It can be seen that, under the operating conditions under investigation, the interfacial hydrogen transport capacity Na decreases as Pm decreases, and vice versa.

[0257] Figure 18 This reflects the effect of the operating pressure Pm of the MIR heavy oil hydrotreating system on the system's pressure-driven hydrogen delivery rate Np. Figure 18 It can be seen that, under the operating conditions under investigation, the system pressure hydrogen transport capacity Np decreases as Pm decreases, and vice versa.

[0258] Figure 19This reflects the influence of the operating pressure Pm of the MIR heavy oil hydrotreating system on the relative magnitudes of the interfacial hydrogen transport capacity Na and the pressure hydrogen transport capacity Np. Figure 19 It can be seen that, under the investigated operating conditions, the Na / Np ratio increases as Pm decreases, and Na is always greater than Np. This means that, under the investigated operating conditions, the interfacial hydrogen transport mechanism is more dominant than the pressure hydrogen transport mechanism in the MIR heavy oil hydrotreating system.

[0259] Table 1 below compares some of the theoretical calculation results for Example 1 (code name E1) and Example 2 (code name E2).

[0260] Table 1 Comparison of some theoretical calculation results between Example 1 and Example 2

[0261]

[0262] As shown in Table 1, changing the structural parameters and operating conditions of the MIR results in different hydrogen mass transfer parameters in the slurry bed heavy oil micro-interface hydrogenation system, which reflects the influence of the MIR structural parameters and operating conditions on the hydrogen transport process.

[0263] According to the two embodiments above Figures 4 to 19 Based on the influence patterns observed and in combination with actual needs, the target design parameters for the slurry bed heavy oil hydrogenation micro-interface reactor are determined.

[0264] This specification provides a device for determining the hydrogen transport rate in a slurry bed heavy oil micro-interface enhanced reaction, which can be used to achieve... Figure 3 The method for determining hydrogen transport in the micro-interface enhancement reaction of slurry-bed heavy oil is shown. For example... Figure 20 As shown, the device includes an acquisition unit 10, a first calculation unit 20, a second calculation unit 30, a third calculation unit 40, a fourth calculation unit 50, and a fifth calculation unit 60.

[0265] The acquisition unit 10 is used to acquire the reactor structural parameters, system physical property parameters, and operating parameters of the slurry bed heavy oil micro-interface enhancement reaction.

[0266] The first calculation unit 20 is used to calculate the energy dissipation rate based on the reactor structural parameters, system physical property parameters, and operating parameters.

[0267] The second calculation unit 30 is used to calculate the bubble size based on the energy dissipation rate.

[0268] The third calculation unit 40 is used to calculate the rising velocity of a single bubble in an infinitely large static liquid phase based on the bubble size.

[0269] The fourth calculation unit 50 is used to calculate the average rising velocity of microbubbles in the micro-interface system based on the rising velocity of a single bubble in an infinitely large static liquid phase.

[0270] The fifth calculation unit 60 is used to calculate the hydrogen transport volume of the micro-interface enhancement reaction of slurry bed heavy oil based on the average rising speed and bubble size of the microbubbles in the micro-interface system.

[0271] In some embodiments, the first computing unit 20 calculates the energy dissipation rate according to the following formula:

[0272]

[0273] Where ε represents the energy dissipation rate within the micro-interface generator, W / kg; λ represents the gas-liquid ratio within the micro-interface generator; ρ L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 V0 represents the volume of the micro-interface generator, in meters. 3 g represents the acceleration due to gravity, 9.81 m / s². 2 H0 represents the internal height of the slurry-bed heavy oil hydrotreating reactor, in meters (m); S0 represents the cross-sectional area of ​​the slurry-bed heavy oil hydrotreating reactor, in square meters (m²). 2 S1 represents the cross-sectional area of ​​the micro-interface generator outlet, in m³. 2 ;P m Q represents the operating pressure, Pa; ΔP represents the pressure difference between the inside and outside of the micro-interface generator, Pa; L0 The volumetric flow rate of fresh heavy oil in a slurry bed heavy oil hydrotreating reactor is expressed in m³. 3 / s.

[0274] In some embodiments, the second calculation unit 30 calculates the bubble size according to the following formula:

[0275]

[0276] d max =0.75(σ L / ρ L ) 0.6 ε -0.4

[0277] d min =11.4(μ) L / ρ L ) 0.75 ε -0.25

[0278] Where, d 32 The diameter of the bubbles in a slurry bed heavy oil micro-interface hydroenhanced reactor is expressed in meters (m). max d min σ represents the maximum and minimum bubble diameters within the micro-interface generator, in meters (m); L The interfacial tension of the gas-liquid interface in a slurry bed heavy oil hydrogenation system is expressed in N / m; ρ LThis represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 μ L ε represents the dynamic viscosity of the liquid phase in the slurry bed heavy oil hydrogenation system, Pa·s; ε represents the energy dissipation rate in the micro-interface generator, W / kg.

[0279] In some embodiments, the third calculation unit 40 calculates the rising velocity of a single bubble in an infinitely large static liquid phase according to the following formula:

[0280]

[0281] Mo = gμ L 4 / ρ L σ L 3

[0282] d e '=d 32 (ρ L g / σ L ) 1 / 2

[0283] Where v0 represents the rising velocity of a single bubble in an infinitely large, static liquid phase, in m / s; and g represents the acceleration due to gravity, 9.81 m / s². 2 μ L The ρ represents the liquid phase dynamic viscosity of the slurry bed heavy oil hydrotreating system, in Pa·s. L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 ;σ L The d represents the interfacial tension between gas and liquid in a slurry bed heavy oil hydrogenation system, in N / m. 32 The K value represents the bubble diameter in a slurry bed heavy oil micro-interface hydroenhanced reactor, in meters (m). b c and n represent empirical constants.

[0284] In some embodiments, the fourth calculation unit 50 calculates the average rising velocity of microbubbles in the micro-interface system according to the following formula:

[0285]

[0286] v G =Q G / S0

[0287] v L =Q L / S0

[0288] Among them, v 32 v0 represents the average rising velocity of microbubbles in the micro-interface system, in m / s; v0 represents the rising velocity of a single bubble in an infinitely large, still liquid, in m / s; v0 GV represents apparent gas velocity, m / s; L Q represents the apparent liquid velocity, in m / s; G The volumetric flow rate of hydrogen at the inlet of a slurry-bed heavy oil hydrotreating reactor, expressed in m³. 3 / s;Q L The volumetric flow rate of heavy oil at the inlet of the slurry bed heavy oil hydrotreating reactor, in m³. 3 / s.

[0289] In some embodiments, the fifth calculation unit 60 calculates the hydrogen transport amount for the slurry bed heavy oil micro-interface enhancement reaction according to the following formula:

[0290]

[0291] Where, N T The amount of hydrogen transported in mol represents the micro-interface enhancement reaction of slurry-bed heavy oil; P m Q represents operating pressure, Pa; G This represents the actual flow rate of gas within the MIG, in meters. 3 / s;H A The Henry's law representing the concentration of hydrogen in heavy oil, expressed in Pa·m. 3 / mol; v 32 The value d represents the average rising velocity of microbubbles in the micro-interface system, in m / s. 32 H0 represents the bubble diameter in the slurry-bed heavy oil micro-interface hydroenhanced reactor (m); H0 represents the internal height of the slurry-bed heavy oil hydroenhanced reactor (m); S0 represents the cross-sectional area of ​​the slurry-bed heavy oil hydroenhanced reactor (m²). 2 ; x represents the mole fraction of hydrogen in heavy oil; ρ L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 M1 represents the average molar mass of heavy oil, in kg / mol.

[0292] In some embodiments, the apparatus further includes a first determining unit and a second determining unit.

[0293] The first determining unit is used to determine the influence of operating pressure on at least one of the following parameters under different values ​​of the target design parameters of the slurry bed heavy oil hydrotreating micro-interface reactor: bubble size of the heavy oil hydrotreating system, gas-liquid interfacial area of ​​the heavy oil hydrotreating system, liquid-side mass transfer coefficient of the heavy oil hydrotreating system, liquid-side volumetric mass transfer coefficient of the heavy oil hydrotreating system, residence time of heavy oil in the reactor of the heavy oil hydrotreating system, hydrogen transport rate based on interfacial hydrogen transport mechanism, hydrogen transport rate based on pressure hydrogen transport mechanism, and the relative magnitude of interfacial hydrogen transport rate and pressure hydrogen transport rate of the heavy oil hydrotreating system.

[0294] The second determining unit is used to determine the values ​​of the target design parameters for the slurry bed heavy oil hydrogenation micro-interface reactor based on the aforementioned influence law.

[0295] The description and function of the above-mentioned device can be understood by referring to the section on the method for determining the hydrogen transport capacity of the micro-interface enhancement reaction of slurry bed heavy oil, and will not be repeated here.

[0296] This invention also provides an electronic device, such as... Figure 21 As shown, the electronic device may include a processor 2101 and a memory 2102, wherein the processor 2101 and the memory 2102 may be connected via a bus or other means. Figure 21 Taking the example of a connection between China and Israel via a bus.

[0297] Processor 2101 may be a central processing unit (CPU). Processor 2101 may also be other general-purpose processors, digital signal processors (DSPs), application-specific integrated circuits (ASICs), field-programmable gate arrays (FPGAs), or other programmable logic devices, discrete gate or transistor logic devices, discrete hardware components, or combinations thereof.

[0298] Memory 2102, as a non-transitory computer-readable storage medium, can be used to store non-transitory software programs, non-transitory computer-executable programs, and modules, such as the program instructions / modules corresponding to the method for determining hydrogen transport in the micro-interface enhancement reaction of slurry-bed heavy oil in this embodiment of the invention (e.g., Figure 20 The calculation unit 10, first calculation unit 20, second calculation unit 30, third calculation unit 40, fourth calculation unit 50, and fifth calculation unit 60 are shown. The processor 2101 executes various functional applications and data processing by running non-transitory software programs, instructions, and modules stored in the memory 2102, thereby realizing the method for determining the hydrogen transport amount of the slurry bed heavy oil micro-interface enhancement reaction in the above method embodiments.

[0299] The memory 2102 may include a program storage area and a data storage area. The program storage area may store the operating system and applications required for at least one function; the data storage area may store data created by the processor 2101, etc. Furthermore, the memory 2102 may include high-speed random access memory and may also include non-transitory memory, such as at least one disk storage device, flash memory device, or other non-transitory solid-state storage device. In some embodiments, the memory 2102 may optionally include memory remotely located relative to the processor 2101, and these remote memories may be connected to the processor 2101 via a network. Examples of such networks include, but are not limited to, the Internet, corporate intranets, local area networks, mobile communication networks, and combinations thereof.

[0300] The one or more modules are stored in the memory 2102, and when executed by the processor 2101, they perform the following: Figure 1 A method for determining the hydrogen transport capacity of the micro-interface enhancement reaction in slurry bed heavy oil in the illustrated embodiment.

[0301] The specific details of the above-mentioned electronic device can be understood by referring to the relevant descriptions and effects in the method embodiments, and will not be repeated here.

[0302] This specification also provides a computer storage medium storing computer program instructions, which, when executed, implement the steps of the method for determining the hydrogen transport volume in the above-described slurry bed heavy oil micro-interface enhancement reaction.

[0303] This specification also provides a computer program product comprising a computer program that, when executed by a processor, implements the steps of the method for determining the hydrogen transport volume in the above-described slurry bed heavy oil micro-interface enhancement reaction.

[0304] Those skilled in the art will understand that all or part of the processes in the methods of the above embodiments can be implemented by a computer program instructing related hardware. The program can be stored in a computer-readable storage medium, and when executed, it can include the processes of the embodiments of the above methods. The storage medium can be a magnetic disk, optical disk, read-only memory (ROM), random access memory (RAM), flash memory, hard disk drive (HDD), or solid-state drive (SSD), etc.; the storage medium can also include combinations of the above types of memory.

[0305] The various embodiments in this specification are described in a progressive manner. For the same or similar parts between the various embodiments, please refer to each other. The focus of each embodiment is to describe the differences from other embodiments.

[0306] The systems, devices, modules, or units described in the above embodiments can be implemented by computer chips or entities, or by products with certain functions.

[0307] For ease of description, the above devices are described separately by function as various units. Of course, in implementing this application, the functions of each unit can be implemented in one or more software and / or hardware.

[0308] As can be seen from the above description of the embodiments, those skilled in the art can clearly understand that this application can be implemented by means of software plus necessary general-purpose hardware platforms. Based on this understanding, the technical solution of this application, in essence, or the part that contributes to the prior art, can be embodied in the form of a software product. This computer software product can be stored in a storage medium, such as ROM / RAM, magnetic disk, optical disk, etc., and includes several instructions to cause a computer device (which may be a personal computer, server, or network device, etc.) to execute certain parts of the methods of various embodiments of this application.

[0309] This application can be used in a wide variety of general-purpose or special-purpose computer system environments or configurations. For example: personal computers, server computers, handheld or portable devices, tablet devices, multiprocessor systems, microprocessor-based systems, set-top boxes, programmable consumer electronics devices, network PCs, minicomputers, mainframe computers, distributed computing environments including any of the above systems or devices, etc.

[0310] This application can be described in the general context of computer-executable instructions, such as program modules, that are executed by a computer. Generally, program modules include routines, programs, objects, components, data structures, etc., that perform a specific task or implement a specific abstract data type. This application can also be practiced in distributed computing environments where tasks are performed by remote processing devices connected via a communication network. In distributed computing environments, program modules can reside in local and remote computer storage media, including storage devices.

[0311] Although this application has been described through embodiments, those skilled in the art will know that this application has many modifications and variations without departing from the spirit of this application, and it is intended that the appended claims cover such modifications and variations without departing from the spirit of this application.

Claims

1. A method for determining the hydrogen transport capacity of a slurry-bed heavy oil micro-interface enhanced reaction, characterized in that, include: To obtain the reactor structural parameters, system physical property parameters, and operating parameters for the micro-interface enhancement reaction of slurry bed heavy oil; The energy dissipation rate is calculated based on the reactor structural parameters, system physical property parameters, and operating parameters. Calculate the bubble size based on the energy dissipation rate; Calculate the rising velocity of a single bubble in an infinitely large static liquid phase based on the bubble size; Calculate the average rising velocity of microbubbles in a micro-interface system based on the rising velocity of a single bubble in an infinitely large static liquid phase. The hydrogen transport capacity of the micro-interface enhancement reaction in slurry bed heavy oil is calculated based on the average rising velocity and bubble size of the microbubbles in the micro-interface system.

2. The method according to claim 1, characterized in that, The energy dissipation rate is calculated based on the reactor structural parameters, system physical property parameters, and operating parameters, including the calculation of the energy dissipation rate using the following formula: Where ε represents the energy dissipation rate within the micro-interface generator, W / kg; λ represents the gas-liquid ratio within the micro-interface generator; ρ L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 V0 represents the volume of the micro-interface generator, in meters. 3 g represents the acceleration due to gravity, 9.81 m / s². 2 H0 represents the internal height of the slurry-bed heavy oil hydrotreating reactor, in meters (m); S0 represents the cross-sectional area of ​​the slurry-bed heavy oil hydrotreating reactor, in square meters (m²). 2 S1 represents the cross-sectional area of ​​the micro-interface generator outlet, in m³. 2 ;P m Q represents the operating pressure, Pa; ΔP represents the pressure difference between the inside and outside of the micro-interface generator, Pa; L0 The volumetric flow rate of fresh heavy oil in a slurry bed heavy oil hydrotreating reactor is expressed in m³. 3 / s.

3. The method according to claim 2, characterized in that, The energy dissipation rate calculation formula is determined based on the following conditions: The MIR operates in a continuous steady-state state. The gas-liquid mixing process inside the MIG is adiabatic and isothermal. The gas decompression process is completed instantaneously, and the pressure inside the MIG is the operating pressure; Neglecting the changes in gas kinetic energy and gravitational potential energy between the gas and liquid phases; The gas is a single-component ideal gas.

4. The method according to claim 1, characterized in that, Calculating the rising velocity of a single bubble in an infinitely large static liquid phase based on bubble size includes calculating the rising velocity of a single bubble in an infinitely large static liquid phase using the following formula: Mo=gμ L 4 / r L s L 3 d e '=d 32 (r L g / s L ) 1 / 2 Where v0 represents the rising velocity of a single bubble in an infinitely large, static liquid phase, in m / s; and g represents the acceleration due to gravity, 9.81 m / s². 2 μ L The ρ represents the liquid phase dynamic viscosity of the slurry bed heavy oil hydrotreating system, in Pa·s. L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 ;σ L The d represents the interfacial tension between gas and liquid in a slurry bed heavy oil hydrogenation system, in N / m. 32 The K value represents the bubble diameter in a slurry bed heavy oil micro-interface hydroenhanced reactor, in meters (m). b c and n represent empirical constants.

5. The method according to claim 1, characterized in that, The hydrogen transport capacity of the slurry bed heavy oil micro-interface enhancement reaction is calculated based on the average rising velocity and bubble size of the microbubbles in the micro-interface system. This includes calculating the average rising velocity of the microbubbles in the micro-interface system using the following formula: v G =Q G / S0 v L =Q L / S0 Among them, v 32 v0 represents the average rising velocity of microbubbles in the micro-interface system, in m / s; v0 represents the rising velocity of a single bubble in an infinitely large, still liquid, in m / s; v0 G V represents apparent gas velocity, m / s; L Q represents the apparent liquid velocity, in m / s; G The volumetric flow rate of hydrogen at the inlet of a slurry-bed heavy oil hydrotreating reactor, expressed in m³. 3 / s;Q L The volumetric flow rate of heavy oil at the inlet of the slurry bed heavy oil hydrotreating reactor, in m³. 3 / s.

6. The method according to claim 1, characterized in that, The hydrogen transport capacity of the micro-interface enhancement reaction in slurry bed heavy oil is calculated based on the average rising velocity and bubble size of the microbubbles in the micro-interface system. This calculation includes using the following formula: Where, N T The amount of hydrogen transported in mol represents the micro-interface enhancement reaction of slurry-bed heavy oil; P m Q represents operating pressure, Pa; G This represents the actual flow rate of gas within the MIG, in meters. 3 / s;H A The Henry's law representing the concentration of hydrogen in heavy oil, expressed in Pa·m. 3 / mol; v 32 The value d represents the average rising velocity of microbubbles in the micro-interface system, in m / s. 32 H0 represents the bubble diameter in the slurry-bed heavy oil micro-interface hydroenhanced reactor (m); H0 represents the internal height of the slurry-bed heavy oil hydroenhanced reactor (m); S0 represents the cross-sectional area of ​​the slurry-bed heavy oil hydroenhanced reactor (m²). 2 ; x represents the mole fraction of hydrogen in heavy oil; ρ L This represents the liquid phase density of a slurry-bed heavy oil hydrogenation system, in kg / m³. 3 M1 represents the average molar mass of heavy oil, in kg / mol.

7. The method according to claim 1, characterized in that, The method further includes: When the target design parameters of the slurry bed heavy oil hydrotreating micro-interface reactor are set to different values, the influence of operating pressure on at least one of the following parameters is determined for each value: bubble size of the heavy oil hydrotreating system, gas-liquid interfacial area of ​​the heavy oil hydrotreating system, liquid-side mass transfer coefficient of the heavy oil hydrotreating system, liquid-side volumetric mass transfer coefficient of the heavy oil hydrotreating system, residence time of heavy oil in the reactor of the heavy oil hydrotreating system, hydrogen transport rate based on interfacial hydrogen transport mechanism, hydrogen transport rate based on pressure hydrogen transport mechanism, and relative magnitude of interfacial hydrogen transport rate and pressure hydrogen transport rate of the heavy oil hydrotreating system. Based on the aforementioned influence patterns, the target design parameters for the slurry-bed heavy oil hydrogenation micro-interface reactor were determined.

8. A device for determining hydrogen transport capacity in a slurry-bed heavy oil micro-interface enhanced reaction, characterized in that, include: The acquisition unit is used to acquire reactor structural parameters, system physical property parameters, and operating parameters for the micro-interface enhancement reaction of slurry bed heavy oil. The first calculation unit is used to calculate the energy dissipation rate based on the reactor structural parameters, system physical property parameters, and operating parameters. The second calculation unit is used to calculate the bubble size based on the energy dissipation rate; The third calculation unit is used to calculate the rising velocity of a single bubble in an infinitely large static liquid phase based on the bubble size. The fourth calculation unit is used to calculate the average rising velocity of microbubbles in the micro-interface system based on the rising velocity of a single bubble in an infinitely large static liquid phase. The fifth calculation unit is used to calculate the hydrogen transport volume of the micro-interface enhancement reaction of slurry bed heavy oil based on the average rising speed and bubble size of the microbubbles in the micro-interface system.

9. An electronic device, characterized in that, include: The system includes a memory and a processor, which are interconnected. The memory stores computer instructions, and the processor executes these computer instructions to implement the method for determining the hydrogen transport volume in the micro-interface enhancement reaction of slurry bed heavy oil as described in any one of claims 1 to 7.

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