A positive displacement hydrogen compressor pump body assembly

Abstract

The present application relates to hydrogen compression pump technical field, disclose a kind of volumetric hydrogen compressor pump body assembly, including compression pump assembly, the output end of compression pump assembly is connected with piston pressure relief piece, the gas outlet end of piston pressure relief piece is connected with cooling tank, the gas outlet end of cooling tank is connected with first pressurizing assembly, the gas outlet end of first pressurizing assembly is connected with secondary pressurizing assembly and storage tank, the gas outlet end of secondary pressurizing assembly and the gas inlet end of storage tank are interconnected, the outside of first pressurizing assembly and secondary pressurizing assembly is equipped with control element.The present application realizes the synchronous acquisition of concentration, corrosion, flow rate, temperature multidimensional risk factors in hydrogen delivery process;Combined with the accurate quantitative calculation of the corrosion area and corrosion depth of pretreatment module, the defects of single monitoring dimension and difficult to accurately identify corrosion risk in the prior art are solved, and potential safety hazards such as hydrogen leakage, pipeline corrosion, flow rate anomaly, temperature fluctuation can be fully captured.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of hydrogen compression pumps, and more particularly to a positive displacement hydrogen compressor pump body assembly. BACKGROUND

[0002] Now, under the trend of global energy structure transformation towards clean and low-carbon, hydrogen energy, as an efficient and zero-emission clean energy carrier, its strategic position is increasingly prominent and is widely used in fuel cell vehicles, industrial hydrogen production, green metallurgy and other fields. As the core key equipment connecting the hydrogen production end and the hydrogen use end in the hydrogen energy industry chain, the positive displacement hydrogen compressor bears the important functions of hydrogen pressurization, pressure stabilization and stable transportation, and its operation stability and safety directly determine the energy efficiency level, operation reliability and safety of the entire hydrogen energy system. With the large-scale development of the hydrogen energy industry, especially the continuous expansion of application scenarios such as hydrogen refueling stations and large-scale green hydrogen projects, higher requirements are put forward for the operation control precision, risk early warning capability and intelligent level of the positive displacement hydrogen compressor.

[0003] However, the existing control technology of the positive displacement hydrogen compressor still has many defects to be solved, which is difficult to meet the current high safety and high precision operation control requirements:

[0004] Firstly, the monitoring dimension of the existing control technology is single, and the comprehensiveness of risk identification is insufficient. The current mainstream compressor control system mainly relies on traditional PLC control architecture, mainly for single-point monitoring and threshold adjustment of basic parameters such as pressure and temperature, and lacks comprehensive perception of multi-dimensional risk factors in the hydrogen delivery process. For example, hydrogen is a flammable and explosive gas, and the risk of concentration exceeding standard after leakage (explosion hazard) is one of the core safety hazards, but the existing technology often lacks accurate monitoring of the hydrogen concentration around the pipeline; at the same time, the compressor and the connecting pipeline are prone to internal wall corrosion during long-term high-pressure hydrogen delivery, which may cause leakage risk, but the existing technology mainly uses single sensor or manual inspection to monitor the corrosion degree of the pipeline, which cannot accurately collect and quantitatively evaluate key parameters such as corrosion area and corrosion depth, making it difficult to identify corrosion risks in a timely and accurate manner.

[0005] Secondly, the risk assessment lacks a systematic quantitative model, and the early warning accuracy is insufficient. The existing technology relies on experience threshold judgment for compressor operation risk assessment, and does not establish a quantitative analysis system for the synergistic effect of multiple risk factors. Different risk factors have different dimensions, and different weights on the overall operation safety, and the existing technology cannot normalize and scientifically weight these risk factors, resulting in strong subjectivity and low accuracy of risk assessment results, making it difficult to truly reflect the actual operation risk level of the compressor. For example, some technologies only realize risk early warning through single parameter overrun alarm, ignoring the superimposed risk that may be caused by multiple parameter abnormality, which is prone to false alarm or missed alarm.

[0006] Thirdly, the risk assessment result is disconnected with the actual operation condition, and lacks a dynamic correction mechanism. The existing risk assessment model is mostly constructed based on theoretical parameters, without fully considering the influence of working condition changes such as pressure fluctuation in the actual operation process of the compressor on the risk level. In actual operation, the pressure fluctuation rate of hydrogen into and out of the gas end may deviate from the theoretical safety fluctuation rate, which will directly lead to the inconsistency between the theoretical risk assessment result and the actual risk level. The existing technology lacks a dynamic correction module for the deviation, cannot realize real-time and accurate calibration of the risk value, and thus affects the reliability of risk early warning and the effectiveness of control strategy.

[0007] Fourthly, the precision and intelligence level of control response are insufficient. The existing compressor control mostly adopts fixed threshold adjustment or simple feedback control, lacks a dynamic regulation and control mechanism based on real-time comprehensive risk value. When multi-dimensional risk factors are abnormally coordinated, accurate adaptive regulation and control cannot be realized according to the risk level, and the processing and output process of risk data in the existing technology is relatively rough, which is difficult to intuitively and timely feed back accurate risk information to the operator, and is not conducive to the rapid disposal of risks and the stable operation of equipment.

[0008] In summary, the existing volumetric hydrogen compressor control technology has problems such as incomplete monitoring dimension, low risk assessment quantification, lack of dynamic correction mechanism, and insufficient control precision, which leads to high safety risk and poor stability in the operation process of the compressor, and is difficult to meet the demand for safe and reliable operation of core equipment in the large-scale development of hydrogen energy industry. Therefore, it becomes a technical problem to be solved in the current hydrogen energy equipment field to develop a volumetric hydrogen compressor pump body assembly capable of realizing accurate multi-dimensional risk monitoring, quantitative assessment and dynamic correction. SUMMARY

[0009] In order to overcome the above-mentioned defects of the prior art, the present application provides a volumetric hydrogen compressor pump body assembly capable of realizing accurate multi-dimensional risk monitoring, quantitative assessment and dynamic correction, which solves the problems in the background art by the following scheme.

[0010] In order to achieve the above-mentioned purpose, the present application provides the following technical scheme: a volumetric hydrogen compressor pump body assembly, comprising a compression pump assembly, an output end of the compression pump assembly being connected with a piston pressure relief piece, an out-gas end of the piston pressure relief piece being connected with a cooling tank, an out-gas end of the cooling tank being connected with a first pressure increasing assembly, an out-gas end of the first pressure increasing assembly being connected with a secondary pressure increasing assembly and a storage tank, the out-gas end of the secondary pressure increasing assembly and the gas delivery end of the storage tank being in communication with each other, the outside of the first pressure increasing assembly and the secondary pressure increasing assembly each being provided with a control piece, the control piece being used for collecting and centrally controlling the operation data of the first pressure increasing assembly and the secondary pressure increasing assembly;

[0011] The control unit includes a data acquisition module, a preprocessing module, a pressure risk control analysis module, a risk output module, a display panel, and a correction module. The output terminal of the data acquisition module is electrically connected to the input terminal of the preprocessing module, the output terminal of the preprocessing module is connected to the input terminal of the pressure risk control analysis module, the output terminal of the pressure risk control analysis module is connected to the input terminal of the correction module, the output terminal of the correction module is connected to the input terminal of the risk output module, and the output terminal of the risk output module is electrically connected to the input terminal of the display panel.

[0012] Preferably, the acquisition module acquires the first pressurization component, which includes a flow rate monitoring sensor, a temperature sensor, a gas detection sensor, a sonar sensor, and a camera.

[0013] Preferably, the acquisition module acquires the first pressurization component to acquire comprehensive hydrogen flow parameters, the flow rate monitoring sensor acquires the gas flow rate at the outlet and inlet within a unit time period, the temperature sensor acquires the gas temperature at the outlet and inlet within a unit time period, the gas detection sensor acquires the hydrogen concentration in the external unit area at the outlet and inlet within a unit time period, and the sonar sensor and camera acquire the corrosion degree of the inner wall of the connecting pipe in the unit area at the outlet and inlet within a unit time period.

[0014] Preferably, the pretreatment module calculates the degree of corrosion on the inner wall of the connecting pipe based on the difference area and corrosion depth. The calculation process is as follows:

[0015] A1. Data Validity Screening: The corrosion depth data collected by the sonar sensor may contain outliers; invalid data must be removed first. Set a depth threshold range: [h] min h max ], where h min h is the minimum measurable depth of the device. max To determine the pipe wall thickness, remove data points exceeding a threshold (hi) and retain only the valid depth dataset H. valid ={h1, h2, ..., h n}, where n is the number of valid measurement points;

[0016] A2. Unit consistency ensures that the units of the difference in area s and depth h match. For example: area s unit: m 2 Depth h (unit: m) 2 ;

[0017] A3. Calculate the average corrosion depth of the effective area:

[0018] The depth of a single measuring point cannot reflect the overall depth level within the area of ​​difference; therefore, it is necessary to calculate the statistical average of the effective depth. The h represents the average corrosion depth within the differential area s. kCorrosion depth of the kth effective measuring point, n is the number of effective measuring points;

[0019] A4, calculating the corrosion degree of the inner wall of the connecting pipe, , the C is the corrosion degree of the inner wall of the connecting pipe, the , respectively are the influence weight of the corrosion area and the corrosion depth on the corrosion degree of the inner wall of the connecting pipe.

[0020] Preferably, the pressure control analysis module is used to calculate the risk value of hydrogen gas pressurized delivery per unit time of the first pressurizing assembly (4), and the calculation process is as follows:

[0021] Step 1: Construct a risk feature vector, denoted as ;

[0022] , the X1 is the maximum over-standard risk of concentration, is the maximum value of the concentration vector, X2 is the maximum corrosion risk of the pipeline, is the maximum value of the corrosion degree vector, X3 is the abnormal difference risk of flow rate, is the 2-norm of the flow rate vector and the design standard vector, X4 is the abnormal difference risk of temperature, is the 2-norm of the temperature vector and the design standard vector;

[0023] Step 2: Construct a normalization matrix M N , in order to eliminate the dimensional differences of each component, such as (X1 unit is %, X3 unit is m / s), a 4×4 diagonal normalization matrix is constructed, and is converted into a dimensionless vector ;

[0024] Step 3: Construct a weight diagonal matrix M W , according to the priority of hydrogen gas delivery risk, set the weight vector , wherein 0.35, 0.3, 0.2 and 0.15 are the conventional values in the industry, and then construct a 4×4 weight diagonal matrix: , the weight matrix is used to weight the normalized feature vector through the diagonal elements, reflecting the importance of each risk factor;

[0025] Step 4: Calculate the theoretical comprehensive risk value R The final risk value is obtained by using vector inner product or matrix multiplication and summation, and the linear algebra expression is: , wherein is a 4-dimensional row vector, which is used to sum the weighted normalized vector, and the result .

[0026] Preferably, the correction module is used to correct the theoretical comprehensive risk value R data.

[0027] Preferably, the correction process is as follows:

[0028] The correction module comprises a pressure acquisition unit and a pressure analysis unit and an actual pressure deviation degree calculation unit, the pressure acquisition unit is used for acquiring the gas pressure value of the gas outlet end and the gas inlet end in a unit time period, the pressure analysis unit is used for calculating the gas pressure fluctuation rate of the gas outlet end and the gas inlet end in a unit time period, and the actual pressure deviation degree calculation unit calculates the deviation degree based on the comparison between the gas pressure fluctuation rate of the gas outlet end and the gas inlet end in a unit time period and the theoretical safe fluctuation rate, and the deviation degree is an actual comprehensive risk value, a correction value is obtained based on the comparison between the comprehensive risk value and the theoretical comprehensive risk value R, the mean value of the correction values obtained based on different time periods is a theoretical correction value, and the real-time comprehensive risk value is calculated according to the theoretical correction value and the theoretical comprehensive risk value R.

[0029] Preferably, the risk output module is used for outputting the real-time comprehensive risk value to a display panel.

[0030] Technical effects and advantages of the present application:

[0031] 1、The present application realizes the synchronous acquisition of the concentration, corrosion, flow rate and temperature multi-dimensional risk factors in the hydrogen conveying process by setting the integrated flow rate monitoring sensor, temperature sensor, gas detection sensor, sonar sensor and camera acquisition module; the accurate quantitative calculation of the corrosion area and corrosion depth is combined with the pretreatment module, the defects that the monitoring dimension is single and the corrosion risk is difficult to accurately identify in the prior art are solved, and potential safety hazards such as hydrogen leakage, pipeline corrosion, abnormal flow rate and temperature fluctuation can be fully captured.

[0032] 2、The present application constructs a multi-dimensional risk feature vector through the pressure risk control analysis module, introduces a normalization matrix to eliminate the dimension difference, combines a weight diagonal matrix to reflect the risk factor priority (concentration > corrosion > flow rate > temperature), establishes a systematic risk quantitative evaluation model, replaces the experience threshold judgment mode in the prior art, effectively avoids the missed judgment and misjudgment problem of the multi-parameter cooperative abnormal superposition risk, makes the risk evaluation result more objective and accurate, and provides reliable data support for safety early warning.

[0033] 3、The present application collects actual pressure parameters through the correction module, calculates the pressure fluctuation rate deviation degree and dynamically corrects the theoretical comprehensive risk value, solves the problem that the risk evaluation in the prior art is disconnected with the actual working condition; the theoretical correction value is obtained based on the mean value of the correction values in multiple time periods, the comprehensive risk value can be calibrated in real time, the risk evaluation result is highly matched with the actual operation state of the compressor, and the timeliness and accuracy of risk early warning are further improved.

[0034] 4、The application constructs a dynamic regulation mechanism based on real-time comprehensive risk value, can realize adaptive control according to risk levels, replaces the fixed threshold adjustment mode of the prior art, intuitively feeds back accurate risk information to a display panel through a risk output module, is convenient for an operator to quickly dispose risks, and cooperates with the collaborative control of the independent control end and the central control module, significantly improves the intelligent degree and stability of compressor operation control, guarantees the safe and efficient operation of the hydrogen energy conveying system, and meets the high safety and high precision operation requirements of core equipment for the large-scale development of the hydrogen energy industry. BRIEF DESCRIPTION OF DRAWINGS

[0035] Figure 1 It is the overall structural schematic diagram of the application;

[0036] Figure 2 It is the side structural schematic diagram of Figure 1 ;

[0037] Figure 3 It is the top view structural schematic diagram of Figure 1 ;

[0038] Figure 4 It is the control block diagram of the control member of the application.

[0039] Reference signs

[0040] 1, compression pump assembly; 2, piston pressure relief member; 3, cooling tank; 4, first pressure assembly; 5, secondary pressure assembly; 6, control member; 7, storage tank. DETAILED DESCRIPTION

[0041] The technical solutions in the embodiments of the application will be clearly and completely described below with reference to the drawings in the embodiments of the application. Obviously, the described embodiments are only part of the embodiments of the application, rather than all the embodiments of the application. Based on the embodiments in the application, all other embodiments obtained by a person of ordinary skill in the art without creative labor fall within the protection scope of the application.

[0042] Referring to the volumetric hydrogen compressor pump body assembly shown in Figures 1-4 , comprising a compression pump assembly 1, the output end of the compression pump assembly 1 is connected with a piston pressure relief member 2, the gas outlet end of the piston pressure relief member 2 is connected with a cooling tank 3, the gas outlet end of the cooling tank 3 is connected with a first pressure assembly 4, the gas outlet end of the first pressure assembly 4 is connected with a secondary pressure assembly 5 and a storage tank 7, and the gas outlet end of the secondary pressure assembly 5 and the gas inlet end of the storage tank 7 are in communication with each other;

[0043] It needs to be specifically pointed out that the connection process of the above-mentioned gas outlet and gas inlet adopts a conventional sealing pipeline for communication, wherein the compression pump assembly 1, the piston pressure relief part 2, the cooling tank 3 and the storage tank 7 are existing structures, the pressurization process of the first pressurization assembly 4 and the secondary pressurization assembly 5 can be realized by a conventional pressurization structure, and the sealing effect of the present embodiment is set to match the effect of the present embodiment.

[0044] It needs to be further pointed out that the structure of the first pressurization assembly 4 and the secondary pressurization assembly 5 is the same, and the present embodiment only sets two groups as an example, the first pressurization assembly 4 and the secondary pressurization assembly 5 are both provided with a control part 6, the control part 6 is used for data acquisition and central control of the first pressurization assembly 4 and the secondary pressurization assembly 5, and the control of the compression pump assembly 1 adopts an independent control end, which is a conventional setting, and the present embodiment is not limited in detail.

[0045] The control part 6 includes a collection module, a preprocessing module, a pressure risk control analysis module, a risk output module, a display panel and a correction module, the output end of the collection module is electrically connected with the input end of the preprocessing module, the output end of the preprocessing module is connected with the input end of the pressure risk control analysis module, the output end of the pressure risk control analysis module is connected with the input end of the correction module, the output end of the correction module is connected with the input end of the risk output module, and the output end of the risk output module is electrically connected with the input end of the display panel.

[0046] The collection module collects the first pressurization assembly 4 including a flow rate monitoring sensor, a temperature sensor, a gas detection sensor, a sonar sensor and a camera; the collection module collects the first pressurization assembly 4 for collecting comprehensive hydrogen flow parameters, the flow rate monitoring sensor is used for collecting the gas flow rate of the gas outlet and the gas inlet in a unit time period, the temperature sensor is used for collecting the gas temperature of the gas outlet and the gas inlet in a unit time period, the gas detection sensor is used for collecting the hydrogen concentration in the external unit area of the gas outlet and the gas inlet in a unit time period, and the sonar sensor and the camera are used for collecting the corrosion degree of the inner wall of the connecting pipe in a unit area of the gas outlet and the gas inlet, which are respectively marked as v1 and v2, t1 and t2, f1 and f2, g1 and g2.

[0047] It needs to be specifically pointed out that the difference area in a unit area collected by the camera is marked as s, and the difference area is derived based on the initial state difference of the connecting pipe, and the sonar sensor is used for collecting the average corrosion depth of the difference area, which is marked as h.

[0048] The preprocessing module calculates the corrosion degree of the inner wall of the connecting pipe based on the difference area and the corrosion depth, and the calculation process is as follows:

[0049] A1, data validity screening: the corrosion depth collected by the sonar sensor may have abnormal values (such as false depth caused by sensor blind area and surface impurities), and invalid data needs to be removed first: set the depth threshold range: [h min , h max ], wherein h min is the minimum measurable depth of the device, and h max is the wall thickness of the connecting pipe (the corrosion depth cannot exceed the wall thickness); remove hi beyond the threshold, and keep the valid depth data set H valid ={h1, h2, …, h n}, n is the number of valid measurement points;

[0050] A2, unit uniformity ensures that the difference area s and the depth h match the units, for example: area s unit: m 2 depth h unit: m 2 ;

[0051] A3, calculate the average corrosion depth of the effective area:

[0052] The depth of a single measurement point cannot reflect the overall depth level in the difference area, and the statistical average value of the effective depth needs to be calculated, , said is the average corrosion depth in the difference area s, h k is the corrosion depth of the kth valid measurement point, and n is the number of valid measurement points;

[0053] A4, calculate the corrosion degree of the connecting pipe inner wall, , said C is the corrosion degree of the connecting pipe inner wall, said , are the influence weights of the corrosion area and the corrosion depth on the corrosion degree of the connecting pipe inner wall, respectively, said s0 and h0 are the baseline values of the normalization processing, and said , The industry weight ratio is usually 0.3 and 0.7;

[0054] The pressure risk analysis module is used to calculate the risk value of hydrogen gas pressurization delivery per unit time of the first pressurization assembly 4, and the calculation process is as follows:

[0055] Step 1: construct a risk feature vector, denoted as ;

[0056] , said X1 is the maximum over-standard risk of concentration (explosion hazard), is the maximum value of the concentration vector (taking the high-risk value at the inlet and outlet), X2 is the maximum corrosion risk of the pipeline (leakage hazard), is the maximum value of the corrosion degree vector, X3 is the abnormal difference risk of flow rate (blockage / leakage), X1 represents the 2-norm (Euclidean distance) between the velocity vector and the design standard vector, and X4 represents the risk of abnormal temperature differences (pressure fluctuations). Let be the 2-norm of the temperature vector and the design standard vector;

[0057] It is necessary to further explain the design of the standard vector. , The industry reference value for the rated flow velocity is 10 m / s; the design standard vector is... , The industry reference value for the rated temperature is 25℃; the 2-norm formula quantifies the degree of general difference between vectors, and this embodiment does not impose specific limitations.

[0058] Step 2: Construct the normalized matrix M N To eliminate the dimensional differences among the components (e.g., X1 in %, X3 in m / s), a 4×4 diagonal normalization matrix is ​​constructed. Transform into a dimensionless vector ;

[0059] Further explanation is needed regarding X1,max. The denominators of each diagonal element represent the maximum permissible value (industry standard value) for the corresponding component: X1,max = 4% (lower explosive limit of hydrogen; exceeding this limit indicates risk saturation); X2,max = 1 (maximum value for corrosion, dimensionless); X3,max is approximately 28.28 m / s (maximum permissible velocity variation norm); X4,max is approximately 77.78℃ (maximum permissible temperature variation norm). Normalization calculation: (Matrix-vector multiplication, with each component independently normalized), result ;

[0060] Step 3: Construct the weight diagonal matrix M W Based on the risk priority of hydrogen transportation (concentration > corrosion > flow rate > temperature), a weight vector is set. The values ​​0.35, 0.3, 0.2, and 0.15 are commonly used values ​​in this industry. A 4×4 weighted diagonal matrix is ​​then constructed: The role of the weight matrix is ​​to weight the normalized feature vector by adding diagonal elements, thereby reflecting the importance of each risk factor.

[0061] Step 4: Calculate the theoretical comprehensive risk value R. The final risk value is obtained using vector dot product or matrix multiplication and summation. The linear algebraic expression is: ,in This is a 4-dimensional row vector, used to sum the weighted normalized vectors. (The higher the value, the higher the risk);

[0062] The correction module is used for correcting the theoretical comprehensive risk value R data, and the correction process is as follows:

[0063] The correction module comprises a pressure acquisition unit, a pressure analysis unit and an actual pressure deviation degree calculation unit, the pressure acquisition unit is used for acquiring the gas pressure values of the gas outlet end and the gas inlet end in a unit time period, the pressure analysis unit is used for calculating the gas pressure fluctuation rate of the gas outlet end and the gas inlet end in a unit time period, and the actual pressure deviation degree calculation unit calculates the deviation degree based on the comparison between the gas pressure fluctuation rate of the gas outlet end and the gas inlet end in a unit time period and the theoretical safe fluctuation rate, the deviation degree is an actual comprehensive risk value, a correction value is obtained based on the comparison between the comprehensive risk value and the theoretical comprehensive risk value R, the mean value of the correction values obtained through multiple calculations in different time periods is a theoretical correction value, and then the real-time comprehensive risk value is calculated according to the theoretical correction value and the theoretical comprehensive risk value R.

[0064] The risk output module is used for outputting the real-time comprehensive risk value to a display panel, wherein the output process of the risk output module and the output process of the display panel are conventional technical means, and the embodiment is not limited in detail.

[0065] It should be noted that, in this document, the terms such as first and second are used only to distinguish one entity or operation from another entity or operation, and do not necessarily require or imply that these entities or operations have any such actual relationship or order. Moreover, the terms "include", "contain" or any other variants thereof are intended to cover non-exclusive inclusion, so that the process, method, article or equipment including a series of elements not only includes those elements, but also includes other elements not explicitly listed or inherent to such process, method, article or equipment.

[0066] Although the embodiments of the present application have been shown and described, it can be understood by those skilled in the art that various changes, modifications, replacements and variations can be made to the embodiments without departing from the principles and spirits of the present application, and the scope of the present application is defined by the appended claims and their equivalents.

Claims

1. A positive-displacement hydrogen compressor pump body assembly, characterized by: The application relates to a hydrogen pressure control system, which comprises a compression pump assembly (1), a piston pressure relief device (2) connected to the output end of the compression pump assembly (1), a cooling tank (3) connected to the gas outlet end of the piston pressure relief device (2), a first pressure assembly (4) connected to the gas outlet end of the cooling tank (3), a secondary pressure assembly (5) and a storage tank (7) connected to the gas outlet end of the first pressure assembly (4), and a control device (6) arranged outside the first pressure assembly (4) and the secondary pressure assembly (5), which is used for collecting and centrally controlling the operation data of the first pressure assembly (4) and the secondary pressure assembly (5). The control device (6) comprises a collecting module, a preprocessing module, a pressure control analysis module, a risk output module, a display panel and a correction module, the output end of the collecting module is electrically connected with the input end of the preprocessing module, the output end of the preprocessing module is connected with the input end of the pressure control analysis module, the output end of the pressure control analysis module is connected with the input end of the correction module, the output end of the correction module is connected with the input end of the risk output module, and the output end of the risk output module is electrically connected with the input end of the display panel. The pressure control analysis module is used for calculating the risk value of hydrogen pressure delivery of the first pressure assembly (4) in unit time, and the calculation process is as follows: Step 1: Constructing the risk feature vector, denoted as ; X1 is the maximum concentration over standard risk, X2 is the maximum corrosion risk of the pipeline, X3 is the abnormal difference risk of the flow rate, X4 is the abnormal difference risk of the temperature, X5 is the abnormal difference risk of the temperature. Step 2: Constructing the normalization matrix M N To eliminate the dimensional differences of each component, a 4x4 diagonal normalization matrix is constructed, which is Transformed into dimensionless vector ; Step 3: Construct the weight diagonal matrix M W According to the priority of hydrogen delivery risk, set the weight vector Then construct the 4x4 weight diagonal matrix: The role of the weight matrix is to weight the normalized eigenvectors through the diagonal elements, reflecting the importance of each risk factor; Step 4: Calculate the theoretical overall risk value R using vector inner product or matrix multiplication and summation to get the final risk value, linear algebra expression is: where is a 4-dimensional row vector, the role is to sum the weighted normalized vector, the result .

2. A positive-displacement hydrogen compressor pump body assembly according to claim 1, wherein: The collecting module collects the first pressure assembly (4) including a flow speed monitoring sensor, a temperature sensor, a gas detection sensor, a sonar sensor and a camera.

3. A positive-displacement hydrogen compressor pump body assembly according to claim 2, wherein: The collecting module collects the first pressure assembly (4) for collecting comprehensive hydrogen flow parameters, the flow speed monitoring sensor is used for collecting the gas flow speed of the gas outlet end and the gas inlet end in a unit time period, the temperature sensor is used for collecting the gas temperature of the gas outlet end and the gas inlet end in a unit time period, the gas detection sensor is used for collecting the hydrogen concentration in the unit area outside the gas outlet end and the gas inlet end in a unit time period, and the sonar sensor and the camera are used for collecting the corrosion degree of the inner wall of the connecting pipe in a unit area of the gas outlet end and the gas inlet end in a unit time period.

4. A positive-displacement hydrogen compressor pump body assembly according to claim 3, wherein: The preprocessing module calculates the corrosion degree of the connecting pipe inner wall based on the difference area and the corrosion depth, and the calculation process is as follows: A1, data validity screening: there are outliers in the corrosion depth collected by the sonar sensor, and invalid data need to be removed: set the depth threshold range: [h min , h max ] where h min is the minimum measurable depth of the device, h max is the wall thickness of the connecting pipe; remove hi beyond the threshold value, and keep the valid depth data set H valid ={h1, h2, …, h n}, n is the number of valid measurement points; A2, the unit ensures the unit matching of the difference area s and the depth h; A3, the effective area average corrosion depth is calculated: The single measurement point depth cannot reflect the overall depth level in the difference area, and the statistical average of the effective depth needs to be calculated, , the is the average corrosion depth in the difference area s, h k The corrosion depth of the kth effective measurement point, n is the number of effective measurement points. A4, calculating the corrosion degree of the inner wall of the connecting pipe, , the C is the corrosion degree of the inner wall of the connecting pipe, the 、 respectively are the influence weight of the corrosion area and the corrosion depth on the corrosion degree of the inner wall of the connecting pipe.

5. A positive-displacement hydrogen compressor pump body assembly according to claim 1, wherein: The correction module is used for correcting the theoretical comprehensive risk value R data.

6. A positive-displacement hydrogen compressor pump body assembly according to claim 5, wherein: The correction process is as follows: The correction module comprises a pressure acquisition unit, a pressure analysis unit and an actual pressure deviation degree calculation unit. The pressure acquisition unit is used to acquire the gas pressure values of the outlet end and the inlet end in a unit time period. The pressure analysis unit is used to calculate the gas pressure fluctuation rate of the outlet end and the inlet end in a unit time period. The actual pressure deviation degree calculation unit calculates the deviation degree based on the comparison between the gas pressure fluctuation rate of the outlet end and the inlet end in a unit time period and the theoretical safe fluctuation rate. The deviation degree is an actual comprehensive risk value. The correction value is obtained based on the comparison between the comprehensive risk value and the theoretical comprehensive risk value R. The correction value mean value obtained based on the multiple calculations in different time periods is a theoretical correction value. The real-time comprehensive risk value is calculated according to the theoretical correction value and the theoretical comprehensive risk value R.

7. A positive-displacement hydrogen compressor pump body assembly according to claim 1, wherein: The risk output module is used to output the real-time comprehensive risk value to the display panel.

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