Water electrolysis hydrogen production purification system modeling method and simulation device

Abstract

The invention discloses a water electrolysis hydrogen production purification system modeling method and simulation device, and the method comprises the steps: building a deoxidation tower model which comprises a deoxidation function module, a flow analysis module and a deoxidation tower temperature analysis module; constructing a cooler and gas-water separator model, and processing outlet fluid parameters of the deoxidation tower model to obtain input parameters of the drying tower model; drying tower models are constructed, the drying tower models comprise a state switching module and first to third drying tower models, and the state switching module controls the first to third drying tower models to be switched according to a working-regeneration-assisting working state; each of the first drying tower model, the second drying tower model and the third drying tower model comprises an adsorption function module, a regeneration function module, an adsorption state flow analysis module, a regeneration state flow analysis module and a drying tower temperature analysis module. According to the method, full-process, multi-equipment and refined modeling of the purification system can be realized, and the requirements of actual engineering or simulation research on the purification model are met.

Description

TECHNICAL FIELD

[0001] The application belongs to the technical field of hydrogen production by water electrolysis, and relates to a modeling method for a hydrogen production by water electrolysis purification system, in particular to a modeling method for a hydrogen production by water electrolysis purification system and a simulation device. BACKGROUND

[0002] Under the background of sustainable development, countries around the world are developing renewable energy technologies. Hydrogen energy has become an important carrier in the energy transition of various countries due to its wide range of uses, high energy density, and strong renewability. The commonly used water electrolysis hydrogen production technology can be divided into four types according to different working principles: alkaline water electrolysis technology (ALK), proton exchange membrane water electrolysis technology (PEM), high-temperature solid oxide water electrolysis technology (SOEC), and solid polymer anion exchange membrane water electrolysis technology (AEM). Among them, the alkaline water electrolysis technology has the longest development time, the most mature technology, and the lowest cost, and is suitable for establishing large-scale water electrolysis hydrogen production projects. PEM water electrolysis hydrogen production technology can adapt to rapid changes in load while having a higher current density, and plays an important role in renewable energy systems. Regardless of which water electrolysis hydrogen production technology is used, the produced hydrogen gas needs to be separated and purified to remove other gas components in the hydrogen gas and improve the purity of the finished hydrogen gas. The water electrolysis hydrogen production purification system includes two links of oxygen removal and drying, and involves oxygen removal towers, coolers, drying towers, gas-water separators, valves and other equipment.

[0003] Existing researches are mostly focused on the internal design and numerical simulation calculation of the related equipment of the purification system, mainly aiming to improve the energy efficiency and purification effect of the equipment. However, there are few modeling studies on the equipment of the water electrolysis hydrogen production purification system, and a relatively perfect modeling method for the water electrolysis hydrogen production purification system has not been developed. Since mechanism modeling can clearly reflect the running status and dynamic characteristics of the equipment, it plays an important role in auxiliary equipment selection, personnel training, fault analysis, and characteristic research. With more and more water electrolysis hydrogen production projects being implemented, the demand for modeling of the whole process of the water electrolysis hydrogen production purification system is increasing. SUMMARY

[0004] The purpose of the present application is to provide a modeling method for a water electrolysis hydrogen production purification system and a simulation device, which can realize modeling of the whole process, multiple devices, and refinement of the purification system, and meet the demand for purification models in actual engineering or simulation research.

[0005] In order to achieve the above purpose, the solution of the present application is:

[0006] A modeling method for a water electrolysis hydrogen production purification system, comprising,

[0007] The deoxidation column model is constructed, and the deoxidation column model includes a deoxidation function module, a flow analysis module and a deoxidation column temperature analysis module, wherein the deoxidation function module takes the deoxidation column inflow gas flow and the inflow gas composition as inputs, calculates the change of the gas composition in the column before and after deoxidation; the flow analysis module takes the deoxidation column inflow gas flow, the inflow gas composition and the hydrogen reaction amount calculated by the deoxidation function module as inputs, calculates the change of the deoxidation column outlet gas flow and composition; and the temperature analysis module takes the deoxidation column outlet gas flow calculated by the flow analysis module and the deoxidation column inflow gas temperature as inputs, calculates the energy transfer and temperature change in the deoxidation column.

[0008] The cooler and the gas-water separator model are constructed, and the outlet fluid parameters of the deoxidation column model are processed to obtain the input parameters of the drying column model.

[0009] The drying column model is constructed, and the drying column model includes a state switching module and a first drying column model to a third drying column model, the state switching module controls the first drying column model to the third drying column model to switch according to the working states of “working-regeneration-assisting”, and the working states of the first drying column model to the third drying column model are all different at any time.

[0010] The first to third drying column models all include an adsorption function module, a regeneration function module, an adsorption state flow analysis module, a regeneration state flow analysis module and a drying column temperature analysis module, wherein the adsorption function module takes the working / auxiliary drying column inflow gas flow and the inflow gas composition as inputs, calculates the working / auxiliary drying column adsorbed water amount change and the change of the gas composition in the column; the regeneration function module takes the regeneration drying column inflow gas flow and the inflow gas composition as inputs, calculates the regeneration drying column desorbed water amount change and the change of the gas composition in the column; the adsorption state flow analysis module takes the working / auxiliary drying column inflow gas flow and the inflow gas composition as inputs and the adsorbed water amount calculated by the adsorption function module as input, calculates the working / auxiliary drying column outlet flow change; the regeneration state flow analysis module takes the regeneration drying column inflow gas flow, the inflow gas composition, the system pressure and the desorbed water amount calculated by the regeneration function module as inputs, calculates the regeneration drying column outlet gas flow and composition change; and the drying column temperature analysis module takes the regeneration drying column outlet flow calculated by the regeneration state flow analysis module and the regeneration drying column inflow gas temperature as inputs, calculates the energy transfer and temperature change in the column.

[0011] The method further includes constructing a parameter correction module, and adjusting the model parameters according to the deviation of the model output variables from the actual data or the set values.

[0012] The flow analysis module of the deoxidation column model has a calculation formula,

[0013] m j,out = n j,out · M j

[0014] wherein,

[0015]

[0016] wherein, m j,out is the mass flow rate of the material j at the outlet of the deoxidizing tower, n j,out is the molar flow rate of the material j at the outlet of the deoxidizing tower, M j is the molar mass of the material j, and j respectively refers to H2, H2O; is the molar flow rate of hydrogen at the outlet of the deoxidizing tower, is the molar flow rate of hydrogen at the inlet of the deoxidizing tower, is the molar flow rate of hydrogen consumed by the reaction, is the molar flow rate of water generated by the reaction; is the molar flow rate of steam at the outlet of the deoxidizing tower, is the molar flow rate of steam at the inlet of the deoxidizing tower.

[0017] wherein the gas flow rate into the deoxidizing tower is,

[0018]

[0019] wherein, n i,in is the molar flow rate of the material i at the inlet of the deoxidizing tower; m in is the mass flow rate at the inlet of the deoxidizing tower; V in is the volume flow rate at the inlet of the deoxidizing tower; p i is the density of the material i at the inlet of the deoxidizing tower; w i is the mass percentage or volume percentage of the material i at the inlet of the deoxidizing tower; M i is the molar mass of the material i, and i respectively refers to H2, O2, H2O; is the molar flow rate of oxygen at the inlet of the deoxidizing tower; is the molar flow rate of water generated by the reaction.

[0020] wherein the deoxidizing tower temperature analysis module of the deoxidizing tower model calculates energy transfer and temperature change, and the heat transfer process in the deoxidizing tower model includes,

[0021]

[0022] wherein, Q1 is the heat transfer amount between the heating wire of the deoxidizing tower and the gas; h1 is the equivalent heat transfer coefficient between the heating wire of the deoxidizing tower and the gas; A1 is the heat transfer area between the heating wire of the deoxidizing tower and the gas; T heat is the temperature of the heating wire of the deoxidizing tower; T in is the temperature of the gas at the inlet of the deoxidizing tower; T outQ1 is the gas temperature at the outlet of the deoxidation tower; Q2 is the heat exchange between the gas and the deoxidation tower shell; A2 is the heat exchange area between the gas and the deoxidation tower shell; h2 is the equivalent heat transfer coefficient between the gas and the deoxidation tower shell; T tower ε is the temperature of the deoxidation tower shell; Q3 is the heat exchange between the heating wire and the deoxidation tower shell; ε is the emissivity of the heating wire; σ is the Stefan-Boltzmann constant; A3 is the radiative heat transfer area between the heating wire and the deoxidation tower shell.

[0023] in,

[0024]

[0025] Q in =η h ·W in

[0026]

[0027] In the formula, Q in To generate heat for the heating wire; C heat For heating wire heat capacity; C tower The heat capacity of the deoxygenation tower body; η h The heating wire electrothermal conversion efficiency; W in C represents the heating power of the heating wire. P,out The specific heat capacity at constant pressure of the gas at the outlet of the deoxidizer; m in C is the inlet mass flow rate of the deoxygenation tower; P,j The isobaric specific heat capacity of substance j at the outlet of the deoxidizer; m j,out Let j be the mass flow rate of substance j at the outlet of the deoxidation tower, where j refers to H2 and H2O respectively.

[0028] When the temperature at the top of the deoxygenation tower exceeds the set value, the heating wire stops heating, and the heating power of the heating wire is 0. When the temperature at the top of the deoxygenation tower is lower than the set value and the temperature of the heating wire is lower than the set value, the heating wire resumes heating, and the heating power of the heating wire is the rated power of the heating wire.

[0029] The expression for the adsorption functional module is as follows:

[0030] m i,in =m in ·ω i

[0031]

[0032] The synchronous iterative adsorption water volume in the working / auxiliary drying tower is:

[0033]

[0034] Where, m i,inmass flow rate of substance i at the inlet of the working / auxiliary drying tower, m in total mass flow rate at the inlet of the working / auxiliary drying tower, ω i mass percentage of substance i in the flow at the inlet of the working / auxiliary drying tower, i respectively refers to H2, O2, H2O; water vapor mass flow rate at the inlet of the working / auxiliary drying tower; adsorbed water amount of the working / auxiliary drying tower; η ad adsorption efficiency of the drying tower; α ad gas residence coefficient;

[0035] The expression of the adsorption state flow analysis module is,

[0036]

[0037] wherein, m out total mass flow rate at the outlet of the working / auxiliary drying tower; water vapor mass flow rate at the outlet of the working / auxiliary drying tower.

[0038] The expression of the regeneration function module is,

[0039]

[0040]

[0041] wherein, m vapor water vapor mass flow rate at the outlet of the regeneration drying tower; k vapor overflow coefficient; p gas pressure in the regeneration drying tower; p s water vapor saturated vapor pressure at the temperature after heating; d is the maximum water content ratio of the gas; M i molar mass of substance i, i respectively refers to H2, H2O; hydrogen mass flow rate at the outlet of the regeneration drying tower;

[0042] obtaining the gas at the outlet of the regeneration drying tower,

[0043]

[0044]

[0045] wherein, water flow rate of hydrogen blown out from the regeneration drying tower; m in mass flow rate at the inlet of the regeneration drying tower; water vapor mass percentage at the inlet of the regeneration drying tower; synchronous iterative liquid storage amount of the regeneration drying tower;

[0046] The expression of the regeneration state flow analysis module is,

[0047]

[0048] In the formula, m is the hydrogen mass percentage at the inlet of the regeneration drying tower; m out m is the mass flow at the outlet of the regeneration drying tower.

[0049] The expression of the drying tower temperature analysis module is,

[0050]

[0051]

[0052] In the formula,

[0053]

[0054] Q in = η h · W in

[0055]

[0056] In the formula, Q1 is the heat exchange amount between the heating wire and the gas; h1 is the equivalent heat exchange coefficient between the heating wire and the gas; A1 is the heat exchange area between the heating wire and the gas; T heat is the temperature of the heating wire; T in is the temperature of the gas at the inlet of the drying tower; T out is the temperature of the gas at the outlet of the drying tower; Q2 is the heat exchange amount between the gas and the drying tower cylinder; A2 is the heat exchange area between the gas and the drying tower cylinder; h2 is the heat exchange coefficient between the gas and the drying tower cylinder; T tower is the temperature of the drying tower cylinder; Q3 is the heat exchange amount between the heating wire and the drying tower cylinder; ε is the emissivity of the heating wire; σ is the Stefan-Boltzmann constant; A3 is the radiation heat exchange area between the heating wire and the drying tower cylinder;

[0057] When the temperature at the upper part of the regeneration drying tower exceeds the set value of the temperature at the upper part of the tower, the heating wire stops heating, at which time the heating power of the heating wire is 0; when the temperature at the upper part of the regeneration drying tower is lower than the set value of the temperature at the upper part of the tower and the temperature of the heating wire is lower than the set value of the temperature of the heating wire, the heating wire resumes heating, at which time the heating power of the heating wire is the rated power of the heating wire.

[0058] The simulation device of the hydrogen purification system for water electrolysis comprises a memory, a processor, and a computer program stored in the memory and executable on the processor; when the processor executes the computer program, the steps of the modeling method of the hydrogen purification system for water electrolysis are implemented.

[0059] After the above scheme, the parameter transmission relationship between each device of the purification system can be clearly determined, the established model can meet the operation requirements of the electrolytic water hydrogen purification system in various scenes such as variable working condition operation, purification state switching, starting and stopping, and provide the change of intermediate parameters, thereby supporting the model demand of the purification system in actual engineering or simulation research. BRIEF DESCRIPTION OF DRAWINGS

[0060] Figure 1 is a schematic diagram of an electrolytic water hydrogen purification system;

[0061] Figure 2 is a flow chart of a modeling method of an electrolytic water hydrogen purification system;

[0062] Figure 3 is a model architecture diagram of a drying tower;

[0063] Figure 4 is a heating control flow chart of a deoxidation tower model;

[0064] Figure 5 is a heating control flow chart of a drying tower model;

[0065] Figure 6 is a purification system operation mode switching control flow chart. DETAILED DESCRIPTION

[0066] The technical solutions and beneficial effects of the present application will be described in detail below with reference to the accompanying drawings.

[0067] The electrolytic water hydrogen purification system modeling method provided by the embodiment of the present application is used for modeling the electrolytic water hydrogen purification system shown in Figure 1 , and the method shown in Figure 2 , the method comprises the following steps.

[0068] S1: Establishing a deoxidation function module, a flow analysis module and a temperature analysis module to constitute a deoxidation tower model of the electrolytic water hydrogen purification system;

[0069] S2: The fluid parameter at the outlet of the deoxidation tower model is processed through a cooler and a steam-water separator model, and then used as an input parameter of a drying tower model;

[0070] S3: Establishing an adsorption function module, a regeneration function module, a state switching module, an adsorption state flow analysis module, a regeneration state flow analysis module and a temperature analysis module to constitute a drying tower model of the electrolytic water hydrogen purification system;

[0071] S4: Establishing a system model parameter correction module in combination with the thermal parameters in the temperature analysis modules of the deoxidation tower and the drying tower;

[0072] As a possible implementation manner of the embodiment, the construction process of the electrolytic water hydrogen purification system model is as follows:

[0073] ① Constructing deoxidizing tower model:

[0074] Since the deoxidizing effect of the existing deoxidizing tower is generally up to ≤1 ppm of oxygen content, it can be considered that the gas stream treated by the deoxidizing tower does not contain oxygen. At the same time, considering the reaction time of the catalytic reaction, the flow resistance of the gas stream in the deoxidizing tower and the macroscopic volume of the deoxidizing tower, it is considered that the gas entering the deoxidizing tower completes the catalytic reaction immediately and flows out of the deoxidizing tower;

[0075] Based on the reaction principle that hydrogen and oxygen react to generate water 2H2+O2=2H2O, the deoxidizing function module takes the flow rate of the gas flowing into the deoxidizing tower and the composition of the gas flowing into the deoxidizing tower as inputs, calculates the change of the composition of the gas in the tower before and after deoxidization, and its model includes:

[0076] The molar flow rate of each component in the gas entering the deoxidizing tower can be calculated according to the mass flow rate or the volume flow rate:

[0077]

[0078]

[0079] In the formula, n i,in is the molar flow rate of substance i at the inlet of the deoxidizing tower; m in is the mass flow rate at the inlet of the deoxidizing tower; V in is the volume flow rate at the inlet of the deoxidizing tower; p i is the density of substance i at the inlet of the deoxidizing tower; w i is the mass percentage or volume percentage of substance i in the flow at the inlet of the deoxidizing tower; M i is the molar mass of substance i; i respectively refers to H2, O2 and H2O; is the molar flow rate of oxygen at the inlet of the deoxidizing tower; is the molar flow rate of water generated by the reaction;

[0080] The deoxidizing tower flow analysis module takes the calculation results of the deoxidizing function module as inputs, and its model includes:

[0081] The mass flow rate of each component in the gas at the outlet of the deoxidizing tower can be expressed as:

[0082] m j,out =n j,out ·M j

[0083] Among them,

[0084]

[0085] In the formula, m j,out is the mass flow rate of substance j at the outlet of the deoxidizing tower, n j,outMj is the molar flow of the material j at the outlet of the deoxidation column j Mj is the molar flow of the material j at the outlet of the deoxidation column Mj is the molar flow of the material j at the outlet of the deoxidation column Mj is the molar flow of the material j at the outlet of the deoxidation column Mj is the molar flow of the material j at the outlet of the deoxidation column Mj is the molar flow of the material j at the outlet of the deoxidation column Mj is the molar flow of the material j at the outlet of the deoxidation column Mj is the molar flow of the material j at the outlet of the deoxidation column

[0086] The deoxidation column temperature analysis module takes the results of the flow analysis module and the temperature of the gas at the inlet of the deoxidation column as inputs, and calculates the energy transfer and temperature change in the deoxidation column. The model includes:

[0087] Since the existing deoxidation column cylinder is covered with a heat preservation layer to prevent heat loss, the heat loss between the cylinder and the environment is ignored. At the same time, the deoxidation column cylinder is regarded as an object with uniform temperature distribution, and the heat transfer process in the deoxidation column can be obtained as follows:

[0088]

[0089]

[0090] In the formula, Q1 is the heat transfer amount between the heating wire and the gas; h1 is the equivalent heat transfer coefficient between the heating wire and the gas; A1 is the heat transfer area between the heating wire and the gas; T heat is the temperature of the heating wire; T in is the temperature of the gas at the inlet of the deoxidation column; T oit is the temperature of the gas at the outlet of the deoxidation column; Q2 is the heat transfer amount between the gas and the cylinder; A2 is the heat transfer area between the gas and the cylinder; h2 is the equivalent heat transfer coefficient between the gas and the cylinder; T tower is the temperature of the deoxidation column cylinder; Q3 is the heat transfer amount between the heating wire and the cylinder; ε is the emissivity of the heating wire; σ is the Stefan-Boltzmann constant; A3 is the radiation heat transfer area between the heating wire and the cylinder; is the fourth power of the temperature of the heating wire; is the fourth power of the temperature of the deoxidation column cylinder;

[0091] wherein,

[0092]

[0093] Q in = η h · W in

[0094]

[0095] In the formula, Ctower Cp is the heat capacity of the deoxidation tower body; Q in W is the heat production of the heating wire; Q in η is the heating power of the heating wire; Q h η is the electric-thermal conversion efficiency of the heating wire; C heat Cp is the heat capacity of the heating wire; C P,out Cp is the constant-pressure specific heat capacity of the mixed gas at the outlet of the deoxidation tower; C P,j Cp is the constant-pressure specific heat capacity of the material j at the outlet of the deoxidation tower; j respectively indicates H2 and H2O;

[0096] When the temperature at the top of the deoxidation tower exceeds the set value, the heating wire stops heating, and at this time, the heating power of the heating wire is 0; when the temperature at the top of the deoxidation tower is lower than the set value and the temperature of the heating wire is lower than the set value, the heating wire resumes heating, and at this time, the heating power of the heating wire is the rated power.

[0097] ②The gas stream output by the deoxidation tower model passes through the cooler model to cool and reduce the gas temperature, thereby reducing the saturated steam pressure of water vapor and the humidity of the gas, liquefying part of the water vapor in the gas, and removing the liquefied water vapor through the gas-water separator model, and finally transmitting the parameters of the processed gas to the drying tower model.

[0098] Among them, the cooler model takes a shell-and-tube heat exchanger as an example, c represents the shell side, t represents the tube side, C p,c Cp is the specific heat capacity of the shell-side fluid; C p,t Cp is the specific heat capacity of the tube-side fluid; m c m is the liquid holdup of the shell side; m t m is the liquid holdup of the tube side; C p,m Cp is the heat capacity of the heat exchanger metal, and the cooler model can be represented as:

[0099]

[0100] T c,avg = T c,in + T c,out

[0101] T t,avg = T t,in + T t,out

[0102] In the formula, h c λ is the convective heat transfer coefficient between the shell-side fluid and the metal; λ c λ is the thermal conductivity between the shell-side fluid and the metal; q m,c q is the inlet working fluid flow rate of the shell side; h ′ c h is the equivalent convective heat transfer coefficient between the shell-side fluid and the metal; h t h is the convective heat transfer coefficient between the tube-side fluid and the metal; λ tk is the heat transfer coefficient between the tube side fluid and the metal; q m,t is the tube side inlet working fluid flow rate; h ′ t is the equivalent convective heat transfer coefficient between the tube side fluid and the metal; T c,in is the shell side inlet working fluid temperature; T c,out is the shell side outlet working fluid temperature; T c,avg is the average temperature of the working fluid inside the shell side; T t,in is the tube side inlet working fluid temperature; T t,out is the tube side outlet working fluid temperature; T t,avg is the average temperature of the working fluid inside the tube side.

[0103] Q c = q m,c · C p,c · (T c,out - T c,in )

[0104] Q t = q m,t · C p,t · (T t,in - T t,out )

[0105] Q1 = h ′ t · (T t,avg - T m )

[0106] Q2 = h ′ c · (T m - T c,avg )

[0107]

[0108] where Q c is the shell side working fluid temperature rise heat transfer rate; Q t is the tube side working fluid temperature drop heat transfer rate; Q1 is the heat transfer rate between the heat exchanger metal and the tube side working fluid; and Q2 is the heat transfer rate between the heat exchanger metal and the shell side working fluid.

[0109] In the gas-water separator model, q in is the two-phase flow rate flowing into the gas-water separator; is the percentage of hydrogen in the gas-water separator inlet material; is the percentage of oxygen in the gas-water separator inlet material; is the percentage of hydrogen in the gas-water separator outlet material; is the percentage of oxygen in the gas-water separator outlet material; is the percentage of water vapor in the gas-water separator outlet material; p gasFor the gas side pressure, the expression of the gas-water separator model is:

[0110]

[0111]

[0112] where d vapor is the humidity of the cooled gas; q vapor is the water vapor flow of the cooled gas; q gas,out is the total flow at the outlet of the gas side of the cooler; p s is the saturated steam pressure at the temperature after cooling.

[0113] The liquid side condensation flow of the gas-water separator is q mbk = q in -q gas,out

[0114] ③ Constructing the drying tower model:

[0115] The drying tower in the hydrogen production purification system is divided into working, auxiliary, and regeneration states. When the drying tower is in the working or auxiliary state, the drying tower adsorbs water vapor, and the liquid storage volume increases synchronously. When the drying tower state switches to the regeneration state, the water accumulated in the previous state is desorbed from the adsorbent after evaporation by heating, and is blown out by dry hydrogen, and the liquid storage volume decreases synchronously.

[0116] The working principles of the working and auxiliary states of the drying tower are the same, that is, the water in the gas is removed by using a porous adsorbent. The working / auxiliary drying tower flow-in gas flow and the composition of the flow-in gas are inputs of the adsorption function module, which calculates the change in the adsorbed water amount and the change in the composition of the gas in the tower. The model can be established as follows:

[0117] m i,in = m in · ω i

[0118]

[0119]

[0120] The synchronous iterative adsorbed water amount in the working / auxiliary drying tower is:

[0121]

[0122] In the formula, m i,in is the mass flow of substance i at the inlet of the working / auxiliary drying tower; ω i is the mass percentage of substance i in the flow at the inlet of the working / auxiliary drying tower; i respectively refers to H2, O2, and H2O; m inThe total mass flow rate at the inlet of the working / auxiliary drying tower; The water vapor mass flow rate at the inlet of the working / auxiliary drying tower; The water adsorbed by the working / auxiliary drying tower; η ad The adsorption efficiency of the drying tower; α ad The gas residence coefficient;

[0123] The adsorption state flow analysis module takes the calculation results of the adsorption function module and the pressure in the drying tower as inputs, and calculates the outlet flow rate variation of the working / auxiliary drying tower. The model can be established as:

[0124]

[0125]

[0126] In the formula, m out The total mass flow rate at the inlet of the working / auxiliary drying tower;

[0127] The working principle of the regeneration drying tower is to use high temperature to vaporize the water adsorbed in the tower, and then blow out the water by the dry gas flow treated by the working drying tower. The regeneration function module takes the inlet gas flow rate and the composition of the inlet gas of the regeneration drying tower as inputs, and calculates the desorption water variation and the gas composition variation in the tower. The model can be established as:

[0128]

[0129] According to Dalton's law of partial pressure, the maximum water content ratio of the gas is:

[0130]

[0131] In the formula, m vapor The water vapor mass flow rate at the outlet of the regeneration drying tower; k vapor The overflow coefficient; p gas The pressure in the drying tower; p s The saturated vapor pressure of water vapor at the temperature after heating; d is the maximum water content ratio of the gas; The hydrogen mass flow rate at the outlet of the regeneration drying tower;

[0132]

[0133]

[0134] In the formula, The water flow rate of hydrogen blown out of the drying tower; m in The total mass flow rate at the inlet of the regeneration drying tower; The water vapor mass percentage at the inlet of the regeneration drying tower; The synchronous iteration liquid storage amount of the drying tower;

[0135] The regeneration state flow analysis module takes the calculation results of the regeneration function module as input, and calculates the regeneration drying tower outlet gas flow and composition change. Its model can be established as:

[0136]

[0137] In the formula, m in is the regeneration drying tower inlet mass flow; is the regeneration drying tower inlet hydrogen mass percentage; m out is the regeneration drying tower outlet mass flow.

[0138] The regeneration drying tower temperature analysis module takes the calculation results of the regeneration state flow analysis module as input, and calculates the tower energy transfer and temperature change. Its model can be established as:

[0139]

[0140]

[0141] wherein,

[0142]

[0143] Q in = η h · W in

[0144]

[0145] In the formula, Q1 is the heat exchange amount between the heating wire and the gas; h1 is the equivalent heat exchange coefficient between the heating wire and the gas; A1 is the heat exchange area between the heating wire and the gas; T heat is the heating wire temperature; T in is the drying tower inlet gas temperature; T out is the drying tower outlet gas temperature; Q2 is the heat exchange amount between the gas and the cylinder; A2 is the heat exchange area between the gas and the cylinder; h2 is the heat exchange coefficient between the gas and the cylinder; T tower is the drying tower cylinder temperature; Q3 is the heat exchange amount between the heating wire and the cylinder; ε is the heating wire emissivity; σ is the Stefan-Boltzmann constant; A3 is the radiation heat exchange area between the heating wire and the cylinder;

[0146] When the regeneration drying tower upper temperature exceeds the tower upper temperature setting value, the heating wire stops heating, at which time the heating wire heating power is 0; when the regeneration drying tower upper temperature is lower than the tower upper temperature setting value and the heating wire temperature is lower than the heating wire temperature setting value, the heating wire resumes heating, at which time the heating wire heating power is the heating wire rated power.

[0147] The drying tower in the working or auxiliary mode uses the adsorption state model, the drying tower in the regeneration mode uses the regeneration state model, and the parameter transmission and the drying tower mode conversion are controlled by the state switching module.

[0148] ④Establishing the system model parameter correction module

[0149] The system model parameter correction module is established by combining the equivalent heat exchange coefficient, heating wire thermal efficiency, heating wire heat capacity, and heating wire emissivity in the deoxidizing tower and the drying tower. The system model parameter correction module adjusts the model parameters according to the deviation of each model output variable from the actual data or the set value.

[0150] As shown in Figure 3 , the drying tower model includes three parts of the working drying tower, the auxiliary drying tower, and the regeneration drying tower. The working and auxiliary drying towers use the adsorption state model, and the regeneration drying tower uses the regeneration state model. The parameters are transmitted between different towers through the state switching module.

[0151] As shown in Figure 4 , the deoxidizing tower temperature control module adopts the dead zone control method. The upper limit set value of the deoxidizing tower temperature is 95℃, and the lower limit of the heating wire temperature is 80℃ when the purification system is running. That is, when the deoxidizing tower temperature is higher than 95℃, the deoxidizing tower heating wire stops heating. When the deoxidizing tower temperature is lower than 95℃ and the heating wire temperature is lower than 80℃, the deoxidizing tower heating wire resumes heating.

[0152] The drying tower model control includes the drying tower working state switching control and the drying tower temperature control. The temperature control is similar to the deoxidizing tower temperature control. The upper limit set value of the regeneration drying tower temperature is 245℃, and the lower limit of the heating wire temperature is 210℃ when the purification system is running. That is, when the regeneration drying tower temperature is higher than 245℃, the regeneration drying tower heating wire stops heating. When the regeneration drying tower temperature is lower than 245℃ and the heating wire temperature is lower than 210℃, the regeneration drying tower heating wire resumes heating.

[0153] Since the drying tower needs to be switched between the adsorption and regeneration states, the working state of a single drying tower is working, auxiliary, and regeneration in turn. The three drying towers in a set of purification system are in different working states, so the working state can be divided into:

[0154] Z1: drying tower A working, drying tower B regeneration, drying tower C auxiliary;

[0155] Z2: drying tower A auxiliary, drying tower B working, drying tower C regeneration;

[0156] Z3: drying tower A regeneration, drying tower B auxiliary, drying tower C working.

[0157] As shown in Figure 5 and Figure 6As shown, by changing the working states Z1, Z2, Z3, corresponding working state instructions are input into the drying tower state switching module, so that the function conversion of the corresponding drying tower can be realized.

[0158] Those skilled in the art will understand that embodiments of the present application can be provided as methods, systems, or computer program products. Therefore, the present application can take the form of an entirely hardware embodiment, an entirely software embodiment, or an embodiment combining software and hardware aspects. Moreover, the present application can take the form of a computer program product implemented on one or more computer-usable storage media (including, but not limited to, disk storage, CD-ROMs, optical storage, etc.) containing computer-usable program code. The solutions in the embodiments of the present application can be implemented in various computer languages, such as the object-oriented programming language Java and the interpreted scripting language JavaScript.

[0159] The present application is described with reference to flowcharts and / or block diagrams of methods, apparatus (systems), and computer program products according to embodiments of the present application. It should be understood that each flow and / or block in the flowcharts and / or block diagrams, as well as combinations of flows and / or blocks in the flowcharts and / or block diagrams, can be implemented by computer program instructions. These computer program instructions can be provided to a processor of a general-purpose computer, a special-purpose computer, an embedded processor, or other programmable data processing apparatus to produce a machine, so that the instructions executed by the processor of the computer or other programmable data processing apparatus generate a means for implementing the functions specified in the flowcharts and / or block diagrams. Figure 1 one or more flows and / or blocks Figure 1 means for carrying out the functions specified in the flowchart

[0160] These computer program instructions can also be stored in a computer-readable memory that can direct the computer or other programmable data processing apparatus to work in a specific manner, so that the instructions stored in the computer-readable memory produce a manufactured product including instruction means, which implements the functions specified in the flowcharts and / or block diagrams. Figure 1 one or more flows and / or blocks Figure 1 means for carrying out the functions specified in the flowchart

[0161] These computer program instructions can also be loaded onto a computer or other programmable data processing apparatus, so that a series of operation steps are performed on the computer or other programmable data processing apparatus to produce a computer-implemented process, so that the instructions executed on the computer or other programmable data processing apparatus provide a means for implementing the functions specified in the flowcharts and / or block diagrams. Figure 1 one or more flows and / or blocks Figure 1 means for carrying out the functions specified in the flowchart

[0162] While the preferred embodiments of the application have been described, additional variations and modifications can be made to these embodiments by those skilled in the art once they have the benefit of the present disclosure without departing from the spirit and scope of the application. Accordingly, it is intended that the appended claims include all such modifications and variations as fall within the scope of the present application.

[0163] It is apparent that those skilled in the art can make various changes and modifications to the application without departing from the spirit and scope of the application. It is therefore intended that the present application cover all such changes and modifications that are within its scope.

Claims

1. A method of modeling a hydrogen purification system for water electrolysis, the method comprising: The method comprises the following steps: ​ A deoxidizing tower model is constructed, which comprises a deoxidizing function module, a flow analysis module and a deoxidizing tower temperature analysis module, wherein the deoxidizing function module takes the deoxidizing tower inflow gas flow and the inflow gas composition as inputs to calculate the change of the gas composition in the tower before and after deoxidization; the flow analysis module takes the deoxidizing tower inflow gas flow, the inflow gas composition and the hydrogen reaction amount calculated by the deoxidizing function module as inputs to calculate the change of the deoxidizing tower outlet gas flow and composition; and the temperature analysis module takes the deoxidizing tower outlet gas flow calculated by the flow analysis module and the deoxidizing tower inflow gas temperature as inputs to calculate the energy transfer and temperature change in the deoxidizing tower; A cooler and a gas-water separator model are constructed to process the deoxidizing tower model outlet fluid parameters to obtain the dry tower model input parameters; A dry tower model is constructed, which comprises a state switching module and first to third dry tower models, the state switching module controls the first to third dry tower models to switch according to the working states of "working-regeneration-assisting", and the working states of the first to third dry tower models are all different at any time.

2. The method of claim 1, wherein the method is characterized by: The first to third dry tower models all comprise an adsorption function module, a regeneration function module, an adsorption state flow analysis module, a regeneration state flow analysis module and a dry tower temperature analysis module, wherein the adsorption function module takes the working / assisting dry tower inflow gas flow and the inflow gas composition as inputs to calculate the change of the working / assisting dry tower adsorbed water amount and the change of the gas composition in the tower; the regeneration function module takes the regeneration dry tower inflow gas flow and the inflow gas composition as inputs to calculate the change of the regeneration dry tower desorbed water amount and the change of the gas composition in the tower; the adsorption state flow analysis module takes the working / assisting dry tower inflow gas flow and the inflow gas composition as inputs and the adsorbed water amount calculated by the adsorption function module as an input to calculate the change of the working / assisting dry tower outlet flow; the regeneration state flow analysis module takes the regeneration dry tower inflow gas flow, the inflow gas composition, the system pressure and the desorbed water amount calculated by the regeneration function module as inputs to calculate the change of the regeneration dry tower outlet gas flow and composition; and the dry tower temperature analysis module takes the regeneration dry tower outlet flow calculated by the regeneration state flow analysis module and the regeneration dry tower inflow gas temperature as inputs to calculate the energy transfer and temperature change in the tower.

3. The method of claim 1, wherein: Further, a parameter correction module is constructed to adjust the model parameters according to the deviation of the model output variables and actual data or set values.

4. The method of claim 1, wherein: The flow analysis module calculation formula of the deoxidizing tower model is: m j,out = n j,out • M j wherein, where m j,out is the mass flow of the material j at the outlet of the deoxidizing column, n j,out is the molar flow of the material j at the outlet of the deoxidizing column, M j is the molar mass of the material j, j respectively H2, H2O; is the molar flow of hydrogen at the outlet of the deoxidizing column, is the molar flow of hydrogen at the inlet of the deoxidizing column, is the molar flow of hydrogen consumed by the reaction, is the molar flow of water produced by the reaction; is the molar flow of water vapor at the outlet of the deoxidizing column, is the molar flow of water vapor at the inlet of the deoxidizing column.

5. The method of claim 4, wherein the method is characterized by: The deoxidizing tower inflow gas flow is: where n i,in is the molar flow of the substance i at the inlet of the deoxidation column; m in is the mass flow at the inlet of the deoxidation column; V in is the volume flow at the inlet of the deoxidation column; p i is the density of the substance i at the inlet of the deoxidation column; w i is the mass or volume percentage of the substance i at the inlet of the deoxidation column; M i is the molar mass of the substance i; i denotes H2, O2, H2O, respectively; is the molar flow of oxygen at the inlet of the deoxidation column; is the molar flow of water produced by the reaction.

6. The method of claim 1, wherein: The deoxidizing tower temperature analysis module of the deoxidizing tower model calculates the energy transfer and temperature change, and the heat transfer process in the deoxidizing tower model comprises: wherein Q1 is the heat exchange amount between the deoxidizing tower heating wire and the gas; h1 is the equivalent heat exchange coefficient between the deoxidizing tower heating wire and the gas; A1 is the heat exchange area between the deoxidizing tower heating wire and the gas; T heat is the deoxidizing tower heating wire temperature; T in is the gas temperature at the deoxidizing tower inlet; T out is the gas temperature at the deoxidizing tower outlet; Q2 is the heat exchange amount between the gas and the deoxidizing tower cylinder; A2 is the heat exchange area between the gas and the deoxidizing tower cylinder; h2 is the equivalent heat exchange coefficient between the gas and the deoxidizing tower cylinder; T tower is the deoxidizing tower cylinder temperature; Q3 is the heat exchange amount between the heating wire and the deoxidizing tower cylinder; ε is the heating wire emissivity; σ is the Stefan-Boltzmann constant; A3 is the radiation heat exchange area between the heating wire and the deoxidizing tower cylinder; wherein, Q in = η h ·W in where Q in is the heat generated by the heating wire; C heat is the heat capacity of the heating wire; C tower is the heat capacity of the deoxidizing tower cylinder; η h is the electric-thermal conversion efficiency of the heating wire; W in is the heating power of the heating wire; C P,out is the constant-pressure specific heat capacity of the gas at the outlet of the deoxidizing tower; m in is the mass flow rate at the inlet of the deoxidizing tower; C P,j is the constant-pressure specific heat capacity of the substance j at the outlet of the deoxidizing tower; m j,out is the mass flow rate of the substance j at the outlet of the deoxidizing tower, j respectively refers to H2 and H2O; When the deoxidizing tower upper temperature exceeds the tower upper temperature set value, the heating wire stops heating, at this time, the heating wire heating power is 0; when the deoxidizing tower upper temperature is lower than the tower upper temperature set value and the heating wire temperature is lower than the heating wire temperature set value, the heating wire resumes heating, at this time, the heating wire heating power is the heating wire rated power.

7. The method of claim 1, wherein: The expression of the adsorption function module is, m i,in = m in · ω i The synchronous iterative adsorption water quantity in the working / auxiliary drying tower is: Wherein, m i,in is the mass flow of substance i at the inlet of the working / auxiliary drying tower, m in is the total mass flow at the inlet of the working / auxiliary drying tower, ω i is the mass percentage of substance i in the inlet flow of the working / auxiliary drying tower, i respectively refers to H2, O2, H2O; is the water vapor mass flow at the inlet of the working / auxiliary drying tower; is the water adsorption amount of the working / auxiliary drying tower; η ad is the drying tower adsorption efficiency; α ad is the gas residence coefficient; The expression of the adsorption state flow analysis module is, where m out is the total mass flow rate of the working / auxiliary drying column outlet; is the mass flow rate of water vapor of the working / auxiliary drying column outlet.

8. The method of claim 1, wherein: The expression of the regeneration function module is, wherein m vapor is the water vapor mass flow at the outlet of the regeneration drying column; k vapor is the overflow coefficient; p gas is the pressure inside the regeneration drying column; p s is the water vapor saturation vapor pressure at the temperature after heating; d is the maximum water content of the gas; M i is the molar mass of the substance i, i respectively H2, H2O; is the hydrogen mass flow at the outlet of the regeneration drying column; The gas at the outlet of the regeneration drying tower is obtained, wherein, m is the water flow rate of hydrogen gas blown out from the regeneration drying tower; in m is the mass flow rate at the inlet of the regeneration drying tower; m is the water vapor mass percentage at the inlet of the regeneration drying tower; m is the synchronous iterative liquid holdup of the regeneration drying tower; The expression of the regeneration state flow analysis module is, wherein is the mass percent of hydrogen at the inlet of the regeneration drying column; m out is the mass flow rate at the outlet of the regeneration drying column.

9. The method of claim 8, wherein: The expression of the drying tower temperature analysis module is, Wherein, Q in = η h ·W in wherein Q1 is the heat transfer between the heating wire and the gas; h1 is the equivalent heat transfer coefficient between the heating wire and the gas; A1 is the heat transfer area between the heating wire and the gas; T heat is the heating wire temperature; T in is the inlet gas temperature of the drying tower; T out is the outlet gas temperature of the drying tower; Q2 is the heat transfer between the gas and the drying tower cylinder; A2 is the heat transfer area between the gas and the drying tower cylinder; h2 is the heat transfer coefficient between the gas and the drying tower cylinder; T tower is the drying tower cylinder temperature; Q3 is the heat transfer between the heating wire and the drying tower cylinder; ε is the emissivity of the heating wire; σ is the Stefan-Boltzmann constant; A3 is the radiation heat transfer area between the heating wire and the drying tower cylinder; When the upper temperature of the regeneration drying tower exceeds the upper temperature setting value, the heating wire stops heating, at which time the heating power of the heating wire is 0; when the upper temperature of the regeneration drying tower is lower than the upper temperature setting value and the temperature of the heating wire is lower than the temperature setting value of the heating wire, the heating wire resumes heating, at which time the heating power of the heating wire is the rated power of the heating wire.

10. An electrolysis water hydrogen purification system simulation device, comprising a memory, a processor, and a computer program stored in the memory and capable of running on the processor; characterized in that: The processor executes the computer program to realize the steps of the electrolytic water hydrogen purification system modeling method according to any one of claims 1 to 9.

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