Distributed measurement method and device for fuel conversion rate and component content in hydrocarbon fuel thermochemical process

Abstract

The invention discloses a distributed measurement method for fuel conversion rate and component content in a hydrocarbon fuel thermochemical process. The method comprises the following steps: pumping a target substance into a reaction tube, and heating to a target temperature required by thermal cracking; relevant parameters are monitored in real time; cooling in real time and collecting gas-phase and liquid-phase substances after thermal cracking of the target substance; analyzing the component distribution of the target substance after thermal cracking on line to obtain the component distribution of the target substance after thermal cracking at different temperatures; changing the pressure, and continuing the above steps to obtain component distribution of the target substance after thermal cracking under different pressures; based on component distribution of a target substance subjected to thermal cracking at different temperatures and different pressures, functions of the conversion rate and the component content of the target substance changing along with the temperature are obtained respectively, and distribution conditions of the conversion rate and the component content of the target substance along a reaction tube are obtained respectively. The invention further discloses a device adopting the method. According to the method and the device, the distributed fuel conversion rate and the content of each component are accurately measured.

Description

Technical Field

[0001] The present invention relates to the fields of thermodynamics, thermodynamics, thermochemistry and supercritical fluid of hydrocarbon fuels, and in particular to a distributed measurement method and device for fuel conversion rate and component content in the thermochemical process of hydrocarbon fuels. Background Art

[0002] Scramjet engines are the main power components of hypersonic vehicles. Under the combined effects of fuel combustion heat release and aerodynamic heating during flight, the engine surface temperature rises sharply, posing a great risk to the safe and stable operation of the aircraft. Active regenerative cooling technology using endothermic hydrocarbon fuel as a combustible coolant to effectively cool and thermally protect key engine parts is the key to ensuring the safe operation of the aircraft. As the Mach number of hypersonic vehicles further increases, the cooling demand of the engine continues to increase, and hydrocarbon fuels need to be further cracked to release more chemical heat sinks. However, the secondary reaction of hydrocarbon fuel cracking products will generate a large amount of coking precursors, which will accumulate on the wall of the cooling channel to form coke, thereby affecting the heat transfer performance of the regenerative cooling system. In severe cases, the cooling channel will be blocked, causing the regenerative cooling system to fail. Therefore, clarifying the degree of cracking of hydrocarbon fuels in the pipeline and the changes in fuel components is of great significance to studying the flow state, convective heat transfer mechanism, mass transfer characteristics, and thermochemical reaction mechanism of hydrocarbon fuels.

[0003] Since the fuel thermal cracking process can be deconstructed into an infinite number of continuous micro-reactions at different fuel conversion rates, Jiang Peixue et al. established a global differential reaction (DGR) model with variable stoichiometric coefficients by means of fluid dynamics simulation and successfully predicted the flow heat transfer process and thermal cracking reaction of n-decane. The DGR model determines the stoichiometric coefficients of each component based on the mass / molar fraction of each component in the thermal cracking experiment of n-decane and takes into account the secondary reactions of some cracking products. For the thermal cracking experiment of n-decane with a fuel conversion rate lower than 24.2%, the prediction error of the model for the mass fraction of cracking products is less than 4.2% (Jiang P, Wang Y, Zhu Y. Differential Global Reaction Model with Variable Stoichiometric Coefficients for Thermal Cracking of n-Decane at Supercritical Pressures[J]. Energy & Fuels, 2019, 33, 7244-7256.).

[0004] Zhang Dingrui et al. conducted a thermal cracking experiment of n-dodecane under supercritical pressure. According to the cracking depth, the thermal cracking of n-dodecane was divided into three stages, namely primary cracking, secondary cracking and deep cracking. For the primary cracking stage with a fuel conversion rate of less than 13%, the author constructed a one-step global reaction kinetics to establish the functional relationship between the mass fraction of the main cracking products and the fuel conversion rate. For the secondary cracking stage, the author further considered the thermal decomposition of alkanes and alkenes and the formation of monocyclic aromatics and cycloolefins. Based on the content of each cracking product component in the primary cracking and secondary cracking stages, the author established a three-dimensional numerical model covering fuel flow heat transfer and thermal cracking reaction. The predicted values ​​of fuel outlet temperature, conversion rate and cracking product distribution are in good agreement with the experimental results, verifying the reliability of the three-dimensional numerical model of primary and secondary thermal cracking of n-dodecane (Zhang D, Hou L, Gao M. Experiment and Modeling on Thermal Cracking of n-Dodecane at Supercritical Pressure[J]. Energy & Fuels, 2018, 32, 12426-12434.).

[0005] Based on the thermal cracking mechanism of n-decane, Zhang Limei et al. established a high-precision model of n-decane cracking reaction with 16 substances and 26 reaction mechanisms, and further investigated the secondary reaction of n-decane at high conversion rate. In the computational fluid dynamics (CFD) simulation, the model is more accurate in predicting fuel conversion rate, temperature and product distribution compared with the global one-step reaction model of n-decane. The model can better reflect the changing trend of the isobaric specific heat and convective heat transfer coefficient of the fluid (Zhang L, Yin R, Wang J. Numerical Investigations on the Molecular Reaction Model for Thermal Cracking of n-Decane at Supercritical Pressures [J]. ACSOmega, 2022, 7, 22351-22362.).

[0006] Ke Tian et al. optimized the RP-3 fuel pyrolysis model based on chemical reaction kinetics and corresponding state principles. After optimization, the model contains 14 species and 6 reaction mechanisms. The calculation results of this model in predicting fuel temperature distribution, species diffusion, thermophysical properties, fluid flow state and coke deposition on the pipeline surface at high conversion rate are almost overlapping with the existing simplified model and the calculation time is reduced by 47.5% (Tian K, Tang Z, Wang J. Simplified Pyrolytic Model of RP-3 Fuel at High Conversion Rates and the Effects of Primary Reaction on the Regenerative Cooling Process [J]. Aerospace Science and Technology, 2022, 129, 7853-7864.).

[0007] The Chinese patent with publication number CN111122652A discloses a method for simplifying the deep cracking model of hydrocarbon fuels. The first simplification basis of this method is the ratio of the reaction rate of each sub-reaction to the reaction rate of the main reaction, and the second simplification basis is to replace the simplified reaction group with a single component. This method can accurately predict the behavior of fuel temperature distribution, component transportation, flow field state and pipeline surface coking, and can significantly improve the calculation efficiency.

[0008] In summary, numerical calculation plays a very important role in the fields of thermochemical reactions, convective heat transfer, etc. However, in general, the number of hydrocarbon fuel cracking product species is large and the cracking kinetics mechanism is complex. The current two-dimensional and three-dimensional numerical calculations only meet the simplified fuel cracking model calculation. However, the simplified method only focuses on the error in the prediction of fuel cracking related parameters, and cannot consider the uncertainty of the rate coefficient in the detailed mechanism and the development state of related parameters in the reaction process, thus affecting the reliability and rationality of the cracking model. Summary of the invention

[0009] The purpose of the present invention is to provide a distributed measurement method and device for fuel conversion rate and component content in the thermochemical process of hydrocarbon fuels, thereby realizing the accurate measurement of distributed fuel conversion rate and the content of each component.

[0010] The present invention provides the following technical solutions:

[0011] A distributed measurement method for fuel conversion rate and component content in a hydrocarbon fuel thermochemical process, the method comprising:

[0012] (1) pumping the target substance into a reaction tube and applying a stable heat flux density to the reaction tube using a DC power supply to heat the target substance to a target temperature required for thermal decomposition;

[0013] (2) Real-time monitoring of the inlet and outlet temperature changes of the target substance, the wall temperature of the reaction tube, and the system pressure at both ends of the reaction tube;

[0014] (3) Real-time cooling and collection of gas and liquid phases of the target substance after thermal cracking;

[0015] (4) using gas chromatography and gas chromatography-mass spectrometry to analyze the component distribution of the target substance after thermal cracking online, and obtaining the component distribution of the target substance after thermal cracking at different temperatures;

[0016] (5) When the reaction tube is cooled to room temperature, the pressure is changed and the above steps (1) to (4) are continued to obtain the component distribution of the target substance after thermal cracking at different pressures;

[0017] (6) Based on the component distribution data of the target substance after thermal cracking at different temperatures and pressures, the functions of the target substance conversion rate and the content of each component changing with temperature are obtained, and further the distribution of the target substance conversion rate and the component content along the reaction tube are obtained.

[0018] In order to avoid the problem that the numerical calculation and simulation of hydrocarbon fuel thermochemical reactions in the past need to simplify the number of fuel species and cracking mechanism, which cannot take into account the uncertainty of the rate coefficient in the detailed mechanism and the development state of related parameters in the reaction process, the present invention proposes a new method for measuring the conversion rate and the content of each component of hydrocarbon fuels based on distributed flow calorimetry. The objects of measurement include the conversion rate of the target substance, the change of the content of each component with temperature, and the conversion rate of the target substance and the distribution of the content of each component along the reaction tube.

[0019] The technical concept of the present invention is as follows: the present invention relies on the distributed flow calorimetry method, assumes that the fuel temperature in each microelement of the reaction tube is equal, and the correlation between the thermal cracking of the fuel and the reaction time can be ignored, and establishes a function of the change of the hydrocarbon fuel conversion rate and the content of each component with the temperature; obtains the temperature distribution of the fuel along the reaction tube through a pre-calibrated temperature-heat sink function, and further obtains the distribution of the conversion rate of the target substance and the content of each component along the reaction tube; thereby establishes the intrinsic connection between the position of the reaction tube where the target substance is located-temperature-conversion rate-content of each component under different pressures.

[0020] The measurement method provided by the present invention is distributed flow calorimetry.

[0021] In step (1), the target substance is selected from one or a combination of at least two of alkanes, olefins, cycloalkanes, cycloolefins or aromatic hydrocarbons.

[0022] Further, in step (1), the target substance is pumped into the reaction tube at a flow rate of 0.1-10 g / s or 1-1000 ml / s, the inner diameter of the reaction tube is 1-6 mm, the length of the reaction tube is 0.5-1.0 m, and the heat flux density applied to the target substance by the DC regulated power supply is 0-1×10 6 W / m 2 , the heating rate is 5-25K / min, and the target temperature required for thermal cracking is 773-1073K.

[0023] Furthermore, in step (3), the gas phase substance after thermal cracking of the target substance comprises hydrogen, alkane compounds, olefin compounds, and alkyne compounds; the liquid phase product after thermal cracking of the target substance comprises alkane compounds, olefin compounds, cycloalkane compounds, cycloolefin compounds, and aromatic hydrocarbon compounds.

[0024] Furthermore, in step (6), the function of the target substance conversion rate changing with temperature is α(T); the function of the content of each component changing with temperature is M i (T); The reaction tube is divided into n micro-elements in advance, and the temperature distribution of the target substance along the reaction tube is calibrated according to the temperature-heat sink function. Assuming that the target substance is isothermal inside each micro-element and the correlation between thermal cracking and reaction time can be ignored, the distribution of the conversion rate of the target substance along the reaction tube is α -1 (T); the distribution of each component content along the reaction tube is M i -1 (T).

[0025] Furthermore, the method further comprises:

[0026] (7) Conduct an accuracy verification experiment on the distribution of the conversion rate and component content of the target substance along the reaction tube: change the length of the reaction tube, maintain the same flow and heat transfer characteristics in each group, and continue steps (1)-(5) to obtain the fuel conversion rate and component distribution of the target substance after thermal cracking under different tube length conditions.

[0027] Furthermore, the accuracy verification experiment of the target substance conversion rate and component content distribution along the reaction tube is as follows: the length of the reaction tube is changed, and each group maintains the same flow and heat transfer characteristics, and the fuel conversion rate and component distribution of the target substance after thermal cracking are obtained under different tube length conditions.

[0028] Furthermore, the flow heat transfer characteristics of the same target material are that the heat flux density applied to each reaction tube by the DC regulated power supply is the same; under the same heat flux density conditions, the error between the wall temperature distribution of the xm reaction tube and the wall temperature distribution of the 1m reaction tube at 0-xm is less than 1.0%.

[0029] Furthermore, the principle of the accuracy verification is that under the same heat flux conditions, the temperature and content distribution of the gas and liquid substances at the outlet of the xm reaction tube are regarded as the reference values ​​of the temperature and content distribution of the gas and liquid substances at the xm position of the 1m reaction tube.

[0030] The present invention also provides a distributed measurement device for the fuel conversion rate and the content of each component of the above method, the measurement device comprising:

[0031] A high-pressure constant-current pump is used to stably pump the target substance to the reaction tube; a liquid flow meter is used to monitor the mass flow of the target substance and the mass flow of the liquid phase substance in real time; a gas flow meter is used to monitor the mass flow of the gas phase substance in real time; a DC regulated power supply is used to input a stable heat flux density into the reaction tube; the reaction tube is used for thermal cracking of the target substance; a thermocouple is used to monitor the fluid outlet temperature in real time; an infrared thermal imager is used to monitor the wall temperature of the reaction tube in real time; a pressure sensor is used to monitor the system pressure in real time; a back-pressure valve is used to provide a stable system pressure; a condenser is used to quickly cool the gas and liquid phase substances of the target substance after thermal cracking; a gas-liquid separation tank is used to separate the gas and liquid phase substances of the target substance after thermal cracking; a gas chromatograph and a gas chromatograph-mass spectrometer are used to analyze the composition of the gas and liquid phase substances of the target substance after thermal cracking; a waste gas and waste liquid recovery device is used to recover the cracked gas and cracked liquid of the target substance;

[0032] The industrial computer is used to execute steps (6) and (7).

[0033] Compared with the prior art, the present invention has the following beneficial effects:

[0034] (1) The present invention uses experimental measurement methods to monitor the changing trend of conversion rate and the evolution of gas and liquid phase substances during fuel cracking, and considers the development state of related substances in the reaction process in detail; on this basis, the intrinsic connection between position-temperature-conversion rate-content of each component is established, which improves the reliability and rationality of the cracking model.

[0035] (2) The present invention provides data support for studying the fuel flow heat transfer mechanism, chemical thermodynamic mechanism, and chemical kinetic mechanism, and provides testing and evaluation methods for the development of new fuels. BRIEF DESCRIPTION OF THE DRAWINGS

[0036] Figure 1 It is a flow chart for measuring the distributed conversion rate and content of each component of hydrocarbon fuels;

[0037] Figure 2 is a schematic diagram of the structure of the measuring device;

[0038] Figure 3 The content of each component of the liquid phase after the cracking of n-decane changes with temperature (3MPa, 1g / s);

[0039] Figure 4 The conversion rate of n-decane changes with temperature when the reaction tube length is 1m (3MPa, 1g / s);

[0040] Figure 5 is the variation of the content of n-decane cracking product (1-pentene) with temperature (3MPa, 1g / s);

[0041] Figure 6 It is the reference value of the conversion rate of n-decane along the reaction tube when the length of the reaction tube is 0.5-1m;

[0042] Figure 7 The change of n-decane conversion rate with temperature under different reaction tube length conditions (3MPa, 1g / s);

[0043] Figure 8 Comparison between the experimental value of n-decane conversion along the process and the reference value (3MPa, 1g / s);

[0044] Fig. 9 Comparison between the experimental value of the content of n-decane cracking product (1-pentene) and the reference value (3MPa, 1g / s). DETAILED DESCRIPTION

[0045] The following examples may enable those skilled in the art to more fully understand the present invention, but do not limit the present invention in any way.

[0046] The process of the distributed measurement method for fuel conversion rate and component content in the thermochemical process of hydrocarbon fuels provided by the present invention is as follows: Figure 1 The structural diagram of the measuring device is shown in Figure 2 As shown, it includes a high-pressure constant current pump, a liquid flow meter, a gas flow meter, a DC regulated power supply, a reaction tube, a thermocouple, an infrared thermal imager, a pressure sensor, a back pressure valve, a condenser, a gas-liquid separation tank, a gas chromatograph, a gas chromatography-mass spectrometer, a waste gas and waste liquid recovery device, and an industrial computer.

[0047] The method for distributed measurement of fuel conversion rate and component content in a hydrocarbon fuel thermochemical process using the measuring device provided by the present invention includes:

[0048] (1) A high-pressure constant-current pump pumps the target substance into the reaction tube; a DC power supply applies a stable heat flux density to the reaction tube to heat the target substance to the target temperature required for thermal cracking.

[0049] (2) Thermocouples monitor the inlet and outlet temperature changes of the target material in real time; infrared thermal imagers monitor the wall temperature of the reaction tube in real time; and pressure sensors monitor the system pressure at both ends of the reaction tube in real time.

[0050] (3) The condenser tube cools the pyrolyzed substances of the target substance in real time; the gas-liquid separation storage tank separates the gas and liquid substances; the gas flow meter and the liquid flow meter respectively monitor the flow rates of the gas and liquid substances in real time.

[0051] (4) The gas chromatograph analyzes the gas-phase substance distribution of the pyrolyzed target substance online; the gas chromatography-mass spectrometry (GC-MS) analyzes the liquid-phase substance distribution of the pyrolyzed target substance online.

[0052] (5) When the reaction tube cools down to room temperature, change the pressure through the back pressure valve, and continue the above steps (1)-(4) to obtain the component distribution of the pyrolyzed target substance under different pressures;

[0053] (6) Based on the component distribution data of the pyrolyzed target substance at different temperatures and pressures detected by the gas chromatograph and the gas chromatography-mass spectrometry, the industrial control computer obtains the functions of the target substance conversion rate and the content of each component changing with temperature, and further obtains the distribution of the target substance conversion rate and the content of each component along the reaction tube; conduct an accuracy verification experiment on the distribution of the target substance conversion rate and the component content along the reaction tube.

[0054] Example 1

[0055] In this example, n-decane is used as the target fluid. Under the conditions of a mass flow rate of 1 g / s, a pressure of 3 MPa, and a reaction tube length of 1 m, n-decane is transported to the reaction tube by a high-pressure constant flow pump and gradually heated from 298 K to 1073 K with a heating step of 25 K; record the magnitude of the heat flux density applied by the DC regulated power supply that changes the temperature; during each heating process, the inlet and outlet temperatures of the fuel and the system pressure in the test tube are measured in real time; when the fuel is heated to the initial pyrolysis temperature (773 K), every 25 K, collect the gas and liquid substances after the fuel pyrolysis; the gas chromatography-mass spectrometry analyzes the liquid-phase substance distribution online to obtain the change of the content of each component in the liquid-phase substance after n-decane pyrolysis with temperature, as Figure 3 shown.

[0056] Relying on the data of the n-decane conversion rate and the content of each component changing with temperature, the industrial control computer obtains the fitting functions of the n-decane conversion rate and the content of each component changing with temperature as Figure 4 and Figure 5 shown;

[0057] The function of the hydrocarbon fuel conversion rate changing with temperature is:

[0058] When T ≤ 823 K, α(T) = 0

[0059] When 823 K < T ≤ 900 K, α(T) = 2066.46 - 4.99·T + 0.0031·T 2 (R = 0.99)

[0060] When 900K < T ≤ 1023K, α(T) = -8271.01 + 16.23·T - 0.0079T 2 (R = 0.99)

[0061] The functions of the contents of each component varying with temperature are as follows: taking 1-pentene as an example

[0062] M(T) = -5810.09 - 26.85·T - 0.0463·T 2 -3.53·10 -5 ·T 3 -1.00·10 -8 ·T 4 (R = 0.99).

[0063] In this embodiment, the length of the reaction tube is gradually shortened in steps of 0.1 m, and the cracking experiments of n-decane are carried out in reaction tubes with lengths of 0.9, 0.8, 0.7, 0.6, and 0.5 m respectively; taking the reaction tube with a length of 0.9 m as an example, the mass flow rate of n-decane, the pressure are maintained the same as those when the length of the reaction tube is 1 m; during the experiment, the heat flux density applied by the DC regulated power supply is always the same as that when the length of the reaction tube is 1 m; under the condition of the same heat flux density for each group, the error between the wall temperature distribution of the x m reaction tube wall and the wall temperature distribution of the 1 m reaction tube at 0 - x m is less than 1.0%; the above conditions are used to ensure that the along - path thermal chemical reaction of the x m tube is similar to the along - path thermal chemical reaction of the 1 m long reaction tube at 0 - x m. The reference values of the along - path conversion rate of n-decane under the condition that the length of the reaction tube is 0.5 - 1 m are as Figure 6 shown. The variation of the conversion rate of n-decane with temperature under different reaction tube lengths is as Figure 7 shown.

[0064] Based on the conversion rate of n-decane, the fitting functions of the contents of each component varying with temperature, and the pre - calibrated n-decane temperature - heat sink curve, the industrial control computer obtains the distributed conversion rate of n-decane and the contents of each component (taking 1-pentene as an example), as Figure 8 and Fig. 9 shown. Compared with the along - path conversion rate of n-decane and the contents of each component obtained from the verification experiment, the relative error of the distributed conversion rate of n-decane is less than 5%, and the relative error of the distributed contents of each component of n-decane (taking 1-pentene as an example) is less than 2%.

Claims

1. A distributed measurement method for fuel conversion rate and component content in the thermochemical process of hydrocarbon fuels, characterized in that: The distributed measurement method comprises: (1) pumping the target substance into a reaction tube and applying a stable heat flux density to the reaction tube using a DC power supply to heat the target substance to a target temperature required for thermal decomposition; (2) Real-time monitoring of the inlet and outlet temperature changes of the target substance, the wall temperature of the reaction tube, and the system pressure at both ends of the reaction tube; (3) Real-time cooling and collection of gas and liquid phases of the target substance after thermal cracking; (4) using gas chromatography and gas chromatography-mass spectrometry to analyze the component distribution of the target substance after thermal cracking online, and obtaining the component distribution of the target substance after thermal cracking at different temperatures; (5) When the reaction tube is cooled to room temperature, the pressure is changed and the above steps (1) to (4) are continued to obtain the component distribution of the target substance after thermal cracking at different pressures; (6) Based on the component distribution of the target substance after thermal cracking at different temperatures and pressures, the functions of the target substance conversion rate and component content changing with temperature are obtained, and further the distribution of the target substance conversion rate and component content along the reaction tube are obtained.

2. The distributed measurement method for fuel conversion rate and component content in the thermochemical process of hydrocarbon fuels according to claim 1 is characterized in that: In step (1), the target substance is selected from one or a combination of at least two of alkanes, olefins, cycloalkanes, cycloolefins or aromatic hydrocarbons.

3. According to the distributed measurement method for fuel conversion rate and component content in the thermochemical process of hydrocarbon fuels in claim 1, in step (1), the flow rate of pumping the target substance into the reaction tube is 0.1-10 g / s or 1-1000 ml / s, the inner diameter of the reaction tube is 1-6 mm, the length of the reaction tube is 0.5-1.0 m, and the heat flux density applied to the target substance by the DC regulated power supply is 0-1×10 6 W / m 2 , the heating rate is 5-25K / min, and the target temperature required for thermal cracking is 773-1073K.

4. According to the distributed measurement method for fuel conversion rate and component content in the thermochemical process of hydrocarbon fuels as described in claim 1, in step (3), the gas phase substance after thermal cracking of the target substance contains hydrogen, alkane compounds, olefin compounds, and alkyne compounds; the liquid phase product after thermal cracking of the target substance contains alkane compounds, olefin compounds, cycloalkane compounds, cycloolefin compounds, and aromatic hydrocarbon compounds.

5. The distributed measurement method for fuel conversion rate and component content in the thermochemical process of hydrocarbon fuels according to claim 1 is characterized in that: In step (6), the function of the target substance conversion rate changing with temperature is α(T); the function of the content of each component changing with temperature is M i (T); the reaction tube is divided into n micro-elements in advance, and the temperature distribution of the target substance along the reaction tube is calibrated according to the temperature-heat sink function; assuming that the target substance is isothermal inside each micro-element and the correlation between thermal cracking and reaction time can be ignored, the distribution of the conversion rate of the target substance along the reaction tube is α -1 (T); the distribution of each component content along the reaction tube is M i -1 (T).

6. The distributed measurement method for fuel conversion rate and component content in the thermochemical process of hydrocarbon fuels according to claim 1 is characterized in that: The method comprises: (7) Conduct an accuracy verification experiment on the distribution of the conversion rate and component content of the target substance along the reaction tube: change the length of the reaction tube, maintain the same flow and heat transfer characteristics in each group, and continue steps (1)-(5) to obtain the fuel conversion rate and component distribution of the target substance after thermal cracking under different tube length conditions.

7. The distributed measurement method for fuel conversion rate and component content in the thermochemical process of hydrocarbon fuels according to claim 6 is characterized in that: The same flow heat transfer characteristics of the target material are that the heat flux density applied to each reaction tube by the DC regulated power supply is the same; under the same heat flux density conditions, the error between the wall temperature distribution of the xm reaction tube and the wall temperature distribution of the 1m reaction tube at 0-xm is less than 1.0%.

8. The distributed measurement method for fuel conversion rate and component content in the thermochemical process of hydrocarbon fuels according to claim 6 is characterized in that: The principle of the accuracy verification is that under the same heat flux conditions, the temperature and content distribution of the gas and liquid phase substances at the outlet of the xm reaction tube are regarded as the reference values ​​of the temperature and content distribution of the gas and liquid phase substances at the xm position of the 1m reaction tube.

9. A device for measuring the distributed conversion rate and the content of each component using the method according to any one of claims 1 to 8, characterized in that: The measuring device comprises: A high-pressure constant-current pump is used to stably pump the target substance to the reaction tube; a liquid flow meter is used to monitor the mass flow rate of the target substance and the mass flow rate of the liquid phase substance in real time; a gas flow meter is used to monitor the mass flow rate of the gas phase substance in real time; a DC regulated power supply is used to input a stable heat flux density into the reaction tube; a reaction tube is used for thermal cracking of the target substance; a thermocouple is used to monitor the fluid outlet temperature in real time; an infrared thermal imager is used to monitor the wall temperature of the reaction tube in real time; a pressure sensor is used to monitor the system pressure in real time; a back pressure valve is used to provide a stable system pressure; a condenser is used to quickly cool the gas and liquid phase substances of the target substance after thermal cracking; a gas-liquid separation tank is used to separate the gas and liquid phase substances of the target substance after thermal cracking; a gas chromatograph and a gas chromatograph-mass spectrometer are used to analyze the composition of the gas and liquid phase substances of the target substance after thermal cracking; a waste gas and waste liquid recovery device is used to recover the cracked gas and cracked liquid of the target substance; An industrial computer is used to execute steps (6) and (7).

Images