A method for optimizing the design of an adsorber

Abstract

The application relates to a high-efficiency optimization design method for an adsorber, and relates to the technical field of the adsorber, which comprises the following steps: acquiring real-time inlet gas density, real-time gas dynamic viscosity, real-time empty tower gas velocity, inlet gas component type and inlet gas component mass concentration; analyzing the real-time inlet gas density, the real-time gas dynamic viscosity and the real-time empty tower gas velocity to determine total pressure drop of an adsorption bed layer; analyzing the real-time empty tower gas velocity, the inlet gas component type and the inlet gas component mass concentration to determine a gas distribution unevenness coefficient; analyzing the total pressure drop of the adsorption bed layer and the gas distribution unevenness coefficient to determine an optimal total flow area; analyzing the optimal total flow area and a preset equal division hole number to determine an equal division hole adjustment parameter; and adjusting equal division holes of an airflow inlet pipe according to the equal division hole adjustment parameter. The application has the effect of improving adsorbent utilization.

Description

Technical Field

[0001] This application relates to the technical field of adsorbers, and in particular to a method for optimizing the design of adsorbers to improve their efficiency. Background Technology

[0002] The composite adsorber is a key unit in the air separation device. Its main task is to remove moisture, carbon dioxide, acetylene and some hydrocarbon impurities from the raw air using a composite adsorption bed, thereby ensuring the safe operation of the subsequent fractionation tower system and preventing the channels from freezing or becoming blocked.

[0003] In related technologies, the side of the airflow inlet pipe of the adsorber is usually perforated so that when the airflow is guided into the adsorber by the airflow inlet pipe, the airflow first passes through the equalization hole, and the equalization hole distributes the airflow evenly into the adsorber, so that the airflow enters the adsorption bed in the radial direction for impurity removal, avoiding the adsorption bed being used too frequently in one direction and too infrequently in another direction.

[0004] Regarding the aforementioned technologies, the uniformly divided holes of the airflow inlet pipe are usually of a fixed diameter. When the impurity concentration in the airflow is too high, the uniformly divided holes of the fixed diameter will cause the airflow velocity to be too fast, and the impurities will be carried out before they can diffuse into the micropores of the adsorbent. When the impurity concentration in the airflow is too low, the uniformly divided holes of the fixed diameter will cause the airflow velocity to be too slow, resulting in an excessively long mass transfer zone and wasted adsorbent capacity, leading to low adsorbent utilization. There is still room for improvement. Summary of the Invention

[0005] To improve the utilization rate of adsorbents, this application provides a method for optimizing the design of adsorbent efficiency.

[0006] In a first aspect, this application provides a method for optimizing the high efficiency of an adsorber, employing the following technical solution: An optimization design method for the high efficiency of an adsorber includes: Obtain real-time intake gas density, real-time gas dynamic viscosity, real-time empty tower gas velocity, intake component type, and intake component mass concentration; The real-time inlet gas density, real-time gas dynamic viscosity, and real-time empty tower gas velocity were analyzed to determine the total pressure drop of the adsorption bed. The real-time empty tower gas velocity, inlet component type, and inlet component mass concentration were analyzed to determine the gas distribution non-uniformity coefficient. The total pressure drop and gas distribution non-uniformity coefficient of the adsorption bed were analyzed to determine the optimal total flow area. The optimal total flow area and the preset number of equal distribution holes are analyzed to determine the adjustment parameters for the equal distribution holes; Adjust the equal distribution holes of the airflow inlet pipe fitting according to the equal distribution hole adjustment parameters.

[0007] Optionally, the steps of analyzing real-time inlet gas density, real-time gas dynamic viscosity, and real-time empty tower gas velocity to determine the total pressure drop of the adsorption bed include: Obtain basic adsorption parameters; Based on a preset viscous resistance model, the basic adsorption parameters, real-time gas dynamic viscosity, and real-time empty tower gas velocity are calculated to generate real-time viscous resistance. Based on a preset inertial drag model, the basic adsorption parameters, real-time inlet gas density, and real-time empty tower gas velocity are calculated to generate real-time inertial drag. The sum of real-time viscous resistance and real-time inertial resistance is calculated to generate the total pressure drop of the adsorption bed.

[0008] Optionally, the steps of analyzing real-time empty tower gas velocity, inlet component type, and inlet component mass concentration to determine the gas distribution non-uniformity coefficient include: The equilibrium adsorption capacity of the components is determined based on the type and mass concentration of the inlet components. The height of the component mass transfer unit is determined based on the type of inlet gas component and the real-time empty tower gas velocity. The component equilibrium adsorption capacity, component mass transfer unit height, real-time empty tower gas velocity, and inlet component mass concentration are substituted into the preset breakthrough time model to determine the actual breakthrough time variable of impurities. The actual penetration time variable of impurities is constrained and solved based on the preset minimum allowable penetration time in order to determine the allowable non-uniformity coefficient of impurities. The permissible non-uniformity coefficients of impurities are sorted to determine the air distribution non-uniformity coefficient.

[0009] Optionally, the steps for determining the equilibrium adsorption capacity of a component based on the type and mass concentration of the inlet component include: Real-time intake temperature and saturated adsorption capacity of components are obtained based on the type of intake components. The Langmuir equilibrium constant of the components is determined based on the type of intake components and the real-time intake temperature. The actual partial pressure of the components is determined based on the mass concentration of the intake components. The saturated adsorption capacity, Langmuir equilibrium constant, and actual partial pressure of the components were analyzed to determine the equilibrium adsorption capacity of the components.

[0010] Optionally, the step of determining the height of the component mass transfer unit based on the inlet component type and the real-time empty tower velocity includes: Determine the maximum local gas velocity variable based on real-time tower gas velocity; Determine the component type correction factor based on the type of intake air components; Obtain the aging correction factor for the adsorbent; The component type correction coefficient, adsorbent aging correction coefficient, maximum local gas velocity variable, and preset baseline mass transfer characteristic coefficient are analyzed to determine the height of the component mass transfer unit.

[0011] Optionally, the steps of analyzing the total pressure drop and gas distribution non-uniformity coefficient of the adsorption bed to determine the optimal total flow area include: The total pressure drop of the adsorption bed is constrained based on the gas distribution non-uniformity coefficient to determine the minimum uniform pressure drop; Obtain real-time airflow volumetric flow rate; The real-time airflow volumetric flow rate and minimum average pressure drop are analyzed to determine the optimal total flow area.

[0012] Optionally, the step of constraining the total pressure drop of the adsorption bed based on the gas distribution non-uniformity coefficient to determine the minimum uniform pressure drop includes: The air distribution non-uniformity coefficient and the preset air distribution structure coefficient are analyzed to determine the uniformity constraint coefficient. Calculate the product of the uniform constraint coefficient and the total pressure drop of the adsorption bed to generate the minimum uniform pressure drop.

[0013] Optionally, the steps of analyzing real-time airflow volumetric flow rate and minimum average pressure drop to determine the optimal total flow area include: The real-time intake density, minimum average pressure drop, and preset orifice flow coefficient are analyzed to determine the flow area conversion ratio coefficient. Calculate the product of the flow-area conversion ratio and the real-time airflow volumetric flow rate to generate the optimal total flow area.

[0014] In summary, this application includes at least one of the following beneficial technical effects: 1. After analyzing the relevant parameters of the air intake, the optimal total flow area is determined. The optimal total flow area is then evenly distributed to all the equal distribution holes to form the equal distribution hole adjustment parameters. The equal distribution holes are adjusted so that the distribution of airflow by the equal distribution holes conforms to the airflow under the current state. Compared with the equal distribution holes with fixed hole diameter, this avoids unnecessary throttling energy waste under low load and low impurity concentration, and also avoids the risk of premature breakthrough caused by insufficient uniformity of air distribution under high load and high impurity concentration, thereby improving the utilization rate of the adsorbent. 2. By starting from the mechanism of adsorption equilibrium thermodynamics and mass transfer kinetics, and using the minimum allowable breakthrough time as a constraint to solve the impurity allowable non-uniformity coefficient in reverse, the abstract gas distribution uniformity requirement is transformed into a quantifiable and calculable value. After sorting all the impurity allowable non-uniformity coefficients, the minimum value is determined as the gas distribution non-uniformity coefficient, ensuring that all impurities meet the breakthrough time constraint, thereby improving the accuracy of the gas distribution non-uniformity coefficient. 3. By analyzing the total pressure drop of the adsorption bed with the gas distribution non-uniformity coefficient as a constraint, the minimum equal distribution pressure drop is obtained. Then, the optimal total flow area is calculated based on the minimum equal distribution pressure drop. The optimization logic of energy consumption optimization under safety constraints is strictly followed. Thus, under the premise of ensuring adsorption breakthrough safety, the throttling pressure drop and operating energy consumption of the equal distribution orifice are reduced to the maximum extent, thereby improving the accuracy of the optimal total flow area. Attached Figure Description

[0015] Figure 1 This is a flowchart of an adsorber efficiency optimization design method in an embodiment of this application.

[0016] Figure 2 This is a flowchart illustrating the steps in this application embodiment to analyze real-time inlet gas density, real-time gas dynamic viscosity, and real-time empty tower gas velocity to determine the total pressure drop of the adsorption bed.

[0017] Figure 3 This is a flowchart of the steps in this application embodiment to analyze the real-time empty tower gas velocity, the type of inlet gas component, and the mass concentration of the inlet gas component to determine the gas distribution non-uniformity coefficient.

[0018] Figure 4 This is a flowchart illustrating the steps for determining the equilibrium adsorption capacity of components based on the type and mass concentration of the intake components in this application embodiment.

[0019] Figure 5 This is a flowchart of the steps for determining the height of the component mass transfer unit based on the type of inlet gas component and the real-time empty tower gas velocity in this embodiment of the application.

[0020] Figure 6 This is a flowchart of the steps in this application embodiment to analyze the total pressure drop and gas distribution non-uniformity coefficient of the adsorption bed to determine the optimal total flow area.

[0021] Figure 7 This is a flowchart of the steps in this application embodiment to constrain the total pressure drop of the adsorption bed based on the gas distribution non-uniformity coefficient in order to determine the minimum uniform pressure drop.

[0022] Figure 8 This is a flowchart of the steps in this application embodiment to analyze the real-time airflow volumetric flow rate and the minimum average pressure drop to determine the optimal total flow area. Detailed Implementation

[0023] To make the purpose, technical solution, and advantages of this application clearer, the following description is provided in conjunction with the appendix. Figures 1 to 8 The present application will be further described in detail below with reference to embodiments. It should be understood that the specific embodiments described herein are for illustrative purposes only and are not intended to limit the scope of the application.

[0024] Reference Figure 1This application discloses a method for optimizing the high efficiency of an adsorber, comprising the following steps: Step S100: Obtain real-time intake gas density, real-time gas dynamic viscosity, real-time empty tower gas velocity, intake component type, and intake component mass concentration.

[0025] When the airflow inlet pipe of the adsorber is perforated with a fixed diameter to form a uniform distribution hole, the uniform distribution hole with a fixed diameter cannot adapt to the operating conditions when the impurity concentration increases or decreases. This can result in either insufficient uniformity of gas distribution and premature penetration of impurities into the adsorption bed, or excessive throttling pressure drop and high operating energy consumption. In order to adapt to the airflow under different operating conditions, it is necessary to dynamically adjust the diameter of the uniform distribution hole. Therefore, it is first necessary to determine the current airflow state, and then detect the real-time inlet gas density, real-time gas dynamic viscosity, real-time empty tower gas velocity, inlet component type, and inlet component mass concentration to provide data support for subsequent adjustment of the uniform distribution hole diameter according to the airflow state.

[0026] The real-time intake air density is the density of the airflow under the current operating conditions. A pressure transmitter and thermometer are installed at the inlet of the airflow inlet pipe to detect the absolute pressure and thermodynamic temperature of the airflow, using the ideal gas law: The calculation yields the following result: For real-time intake air density, The absolute pressure of the airflow. The temperature is the thermodynamic temperature of the airflow. The average molar mass of air is 0.029. For example, As the universal gas constant, 8.314 For example.

[0027] Real-time gas dynamic viscosity is a parameter reflecting the viscous frictional characteristics of the gas under current operating conditions, and its unit is 1000 liters. The result was obtained using the Sutherland empirical formula: In the formula, For real-time gas dynamic viscosity, As a reference viscosity, For example, The temperature is the thermodynamic temperature of the airflow. For reference temperature, 273.15 For example, For example, 110.4 is the Sutherland constant for air.

[0028] The real-time empty tower gas velocity is the average apparent gas flow velocity of the adsorption bed cross-section. A flow meter is installed at the inlet of the gas inlet pipe to detect the total gas flow rate. The operator determines the actual bed cross-sectional area based on the adsorber bed. In the formula, For real-time tower air velocity, This represents the total gas flow rate. This represents the actual cross-sectional area of ​​the bed.

[0029] The intake component type is the type of impurities in the current operating airflow, including moisture, carbon dioxide, acetylene, and various hydrocarbons. Moisture is detected using a mirror dew point meter, while carbon dioxide and hydrocarbons are detected using an online chromatograph. The corresponding impurity type is matched based on the peak retention time.

[0030] The mass concentration of the intake component is the mass concentration of various types of impurities in the airflow under the current operating conditions. After the volume concentration or molar concentration of the impurities is obtained by online analysis instruments, it is converted into mass concentration by combining the ideal gas law.

[0031] Step S101: Analyze the real-time inlet gas density, real-time gas dynamic viscosity, and real-time empty tower gas velocity to determine the total pressure drop of the adsorption bed.

[0032] The total pressure drop of the adsorption bed is the inherent resistance loss caused by the airflow passing through the adsorption bed. It is calculated by the treatment terminal based on the real-time inlet gas density, real-time gas dynamic viscosity, and real-time empty tower gas velocity. The specific method is described in [reference needed]. Figure 2 The steps are as follows. Due to differences in packing density and adsorbent particle size, the resistance to airflow varies at different locations in the adsorption bed. Airflow naturally converges at locations with lower resistance, resulting in uneven gas velocity distribution across the adsorption bed cross-section. The adjustable aperture of the distribution holes effectively acts as a common damper in series along the airflow path. A larger common damper reduces the impact of differences in adsorption bed resistance on gas velocity distribution, leading to more uniform gas distribution. The total pressure drop of the adsorption bed provides data support for subsequently determining the optimal total flow area based on the gas distribution non-uniformity coefficient.

[0033] Step S102: Analyze the real-time empty tower gas velocity, inlet component type, and inlet component mass concentration to determine the gas distribution non-uniformity coefficient.

[0034] The gas distribution non-uniformity coefficient is a quantitative value representing the uniformity of gas velocity distribution in the adsorption bed. It is calculated by the processing terminal based on real-time empty tower gas velocity, inlet component type, and inlet component mass concentration. The specific method is described in [reference needed]. Figure 3 The steps are as follows. The higher the pressure drop of the evenly distributed holes, the more uniform the gas distribution and the smaller the gas distribution non-uniformity coefficient. Non-uniform gas distribution will cause the local gas velocity in the adsorption bed to increase. On the one hand, it will accelerate the local impurity input flux and make the adsorbent saturate faster. On the other hand, it will increase the local mass transfer resistance, lengthen the mass transfer zone, and compress the effective adsorption bed thickness. The dual effect will cause the local area to penetrate prematurely. Therefore, a smaller gas distribution non-uniformity coefficient is required.

[0035] Step S103: Analyze the total pressure drop and gas distribution non-uniformity coefficient of the adsorption bed to determine the optimal total flow area.

[0036] The optimal total flow area is the effective flow area of ​​the evenly distributed orifices adapted to the current airflow conditions. It is obtained by analyzing and calculating the total pressure drop and gas distribution non-uniformity coefficient of the adsorption bed at the treatment terminal. The specific method is described in [reference needed]. Figure 6 The steps are as follows. The optimal total flow area avoids unnecessary throttling losses due to an excessively small flow area, and also avoids uneven gas distribution and premature penetration of impurities into the adsorption bed due to an excessively large flow area.

[0037] Step S104: Analyze the optimal total flow area and the preset number of equal distribution holes to determine the adjustment parameters for the equal distribution holes.

[0038] The number of equal distribution holes refers to the total number of equal distribution holes on the airflow inlet pipe, which is determined by the processing terminal based on the actual situation of the equal distribution holes.

[0039] The equalization orifice adjustment parameter is the adjustment opening of the equalization orifice. The processing terminal calculates the quotient of the optimal total flow area and the number of equalization orifices to obtain the flow area of ​​each equalization orifice. Then, the quotient of the flow area and the reference area of ​​the equalization orifice is calculated to obtain the opening of the equalization orifice, which is the equalization orifice adjustment parameter.

[0040] Step S105: Adjust the equal distribution hole of the airflow inlet pipe according to the equal distribution hole adjustment parameters.

[0041] After determining the equalization orifice adjustment parameters, the processing terminal controls the electric valve group to adjust the orifice diameter according to the opening degree corresponding to the equalization orifice adjustment parameters, thereby ensuring that the equalization orifice provides an accurate pressure drop. On the one hand, it will not cause uneven gas distribution in the adsorption bed due to too small a pressure drop, causing the gas flow to penetrate the adsorption bed prematurely. On the other hand, it will not cause unnecessary throttling losses due to too large a pressure drop.

[0042] Reference Figure 2 The steps for determining the total pressure drop of the adsorption bed by analyzing real-time inlet gas density, real-time gas dynamic viscosity, and real-time empty tower gas velocity include: Step S200: Obtain basic adsorption parameters.

[0043] Among them, the basic adsorption parameters are the parameters related to the adsorption bed and the bed resistance to airflow, including the adsorption bed height, adsorption bed porosity, and adsorbent particle diameter.

[0044] The adsorption bed height is the effective penetration height of the adsorption bed inside the adsorber. It can be either radial or axial, depending on the type of adsorber. It is measured by the operator multiple times and the average value is taken.

[0045] The porosity of the adsorption bed is the ratio of the pore volume between adsorbent particles in the adsorption bed to the total volume of the bed. Adsorbent particles of the same type and from the same batch are compacted and stacked in the same way. The volume after compaction is measured, the mass of the adsorbent particles is weighed, and the volume of the adsorbent particles is calculated based on the density of the adsorbent particles. The pore volume is obtained by subtracting the volume of the adsorbent particles from the volume after compaction. The initial porosity is obtained by calculating the quotient of the pore volume and the volume after compaction. After multiple measurements and calculations, the average value of the initial porosity is obtained to obtain the porosity of the adsorption bed.

[0046] The adsorbent particle diameter is the equivalent diameter when the adsorbent particles are converted into spherical particles of equal volume. The operator actually measures the volume of the adsorbent particles and then solves for the adsorbent particle diameter by combining the spherical volume formula with the volume of the adsorbent particles.

[0047] Step S201: Calculate the adsorption basic parameters, real-time gas dynamic viscosity, and real-time empty tower gas velocity based on the preset viscous resistance model to generate real-time viscous resistance.

[0048] The viscous resistance model is used to calculate real-time viscous resistance, and its specific expression is as follows: .

[0049] In the formula, For real-time viscous resistance, This refers to the adsorption bed height in the basic adsorption parameters. For real-time gas dynamic viscosity, The porosity of the adsorption bed is a fundamental parameter in adsorption. For real-time tower air velocity, The diameter of the adsorbent particles is a fundamental parameter in adsorption.

[0050] This model is derived based on the Kozeny-Carman laminar flow theory. The airflow in the adsorption bed is in a laminar state, and the flow channel is equivalent to a series of tortuous capillary tubes. The laminar flow in a single tube is restrained by Poiseuille's law, and the pressure drop inside the tube is... With flow rate Viscosity Inversely proportional to pipe diameter Inversely proportional to the square: In the formula For pipe length, and flow velocity The relationship with the real-time tower velocity is as follows: Pipe diameter According to the definition of hydraulic radius, we can obtain Introducing tortuosity Correct pipe length ,Right now Substituting into Poiseuille's formula, we get Finally, by performing linear regression on hundreds of fixed-bed pressure drop test data with different particle sizes, porosities, and flow properties, the tortuosity and the prior geometric coefficient were merged into a unified constant, taking 150 as an example.

[0051] Real-time viscous resistance is the pressure loss caused by the viscous friction between gas molecules and the surface of adsorbent particles when the gas flows through the adsorption bed under the current gas flow conditions. It is calculated by the processing terminal by substituting the real-time gas dynamic viscosity, real-time empty tower gas velocity, adsorption bed height, adsorption bed porosity, and adsorbent particle diameter into the viscous resistance model.

[0052] Step S202: Calculate the basic adsorption parameters, real-time intake density, and real-time empty tower gas velocity based on the preset inertial drag model to generate real-time inertial drag.

[0053] The inertial drag model is used to calculate real-time inertial drag, and its specific expression is as follows: .

[0054] In the formula, For real-time inertial drag, For real-time intake air density, This refers to the adsorption bed height in the basic adsorption parameters. The porosity of the adsorption bed is a fundamental parameter in adsorption. For real-time tower air velocity, The diameter of the adsorbent particles is a fundamental parameter in adsorption.

[0055] This model is derived based on the Burke-Plummer turbulent drag theory. At high air velocities, drag is mainly determined by boundary layer separation, vortex formation, and inertial momentum loss as the airflow passes over a particle. When the airflow surrounds a single particle, the inertial drag is proportional to the fluid dynamic head, i.e. , The actual flow velocity within the pores. The number of particles per unit bed volume is The total resistance per unit volume of bed is the product of the resistance of a single particle and the total number of particles. Therefore, after simplification, we get... After regression analysis of a large amount of fixed-bed pressure drop experimental data in a sufficiently turbulent region, the pre-proportional coefficient was found to be 1.75.

[0056] Real-time inertial drag is the morphological drag loss caused by the continuous contraction, turning, expansion and collision of the airflow as it passes through the adsorption bed under the current airflow conditions. It is calculated by the processing terminal by substituting the real-time inlet density, real-time empty tower velocity, adsorption bed height, adsorption bed porosity and adsorbent particle diameter into the inertial drag model.

[0057] Step S203: Calculate the sum of real-time viscous resistance and real-time inertial resistance to generate the total pressure drop of the adsorption bed.

[0058] In this step, the total pressure drop of the adsorption bed is consistent with that in step S101, and is obtained by calculating the sum of the real-time viscous resistance and the real-time inertial resistance from the processing terminal.

[0059] Reference Figure 3 The steps for determining the gas distribution non-uniformity coefficient by analyzing real-time empty tower gas velocity, inlet gas component type, and inlet gas component mass concentration include: Step S300: Determine the equilibrium adsorption capacity of the components based on the type and mass concentration of the inlet components.

[0060] The component equilibrium adsorption capacity is the mass of impurities that a unit mass of adsorbent can adsorb when adsorption equilibrium is reached. It is obtained by analyzing the type and concentration of the inlet air components at the treatment terminal. Specific methods are described in [reference needed]. Figure 4 The steps.

[0061] Step S301: Determine the height of the component mass transfer unit based on the type of inlet component and the real-time empty tower gas velocity.

[0062] The height of the component mass transfer unit is a quantified value of the adsorption mass transfer resistance. A smaller component mass transfer unit height results in higher mass transfer efficiency and a shorter mass transfer zone. This height is obtained by analyzing the inlet component type and real-time orifice gas velocity at the processing terminal. Specific methods are described in [reference needed]. Figure 5 The steps.

[0063] Step S302: Substitute the component equilibrium adsorption capacity, component mass transfer unit height, real-time empty tower gas velocity, and inlet component mass concentration into the preset breakthrough time model to determine the actual breakthrough time variable of impurities.

[0064] The breakthrough time model is a model for determining the actual breakthrough time variable of impurities, and its specific expression is as follows: .

[0065] In the formula, The actual penetration time of impurities is a variable. The preset adsorbent packing density, To achieve the equilibrium adsorption capacity of the components, The preset adsorbent bed height, The preset average saturation coefficient of the mass transfer region. For the height of the component mass transfer unit, The preset number of mass transfer units, Allow for non-uniformity coefficients for impurities. For real-time tower air velocity, This represents the mass concentration of the intake components.

[0066] because Therefore, the only unknown in the penetration time model is the impurity allowable non-uniformity coefficient variable. Therefore, it can be used to include The expression represents the actual penetration time variable.

[0067] The adsorption bed is divided into an upstream saturated adsorbent and a downstream mass transfer zone along the airflow direction. The breakthrough time is the ratio of the total effective adsorption capacity to the impurity input capacity. In the saturated zone, the adsorbent reaches its component equilibrium adsorption capacity. At this time, the impurity concentration in the mass transfer zone gradually decreases from the inlet concentration, the adsorbent is not completely saturated, and the average adsorption capacity is close to the saturation value. Times. Mass transfer region height Therefore, the total effective adsorption mass per unit bed cross-sectional area is After sorting, we get The formula uniformly adopts The average saturation coefficient of the mass transfer region is used to obtain the molecular weight. The gas velocity in the locally high-velocity region is equal to the average gas velocity. Therefore, the mass of impurities passing through a unit cross-sectional area per unit time is times, and thus the mass of impurities passing through a unit cross-sectional area per unit time is... Using this as the denominator, we obtain the penetration time model.

[0068] The adsorbent bulk density is the mass of adsorbent per unit bed volume, which is obtained by measuring the average value of the tightly packed adsorbent using the standard graduated cylinder method.

[0069] The height of the adsorbent bed is the total height of the adsorption bed, which is measured by the operator.

[0070] The average saturation coefficient of the mass transfer zone is a coefficient that reflects the average saturation degree of the adsorbent in the mass transfer zone. It is obtained by fitting and measuring the dynamic breakthrough test. Taking 0.5 as an example of the symmetrical breakthrough curve, the height of the mass transfer zone is first calculated from the breakthrough characteristic time, and then the total adsorption capacity of the bed is obtained by integrating the breakthrough curve. After deducting the adsorption capacity of the saturated zone, the value is obtained by comparing it with the theoretical maximum adsorption capacity of the mass transfer zone when it is completely saturated.

[0071] The number of mass transfer units is the number of mass transfer units of impurities, determined by the breakthrough concentration threshold and adsorption equilibrium characteristics. It reflects the difficulty of separating impurities in the adsorbent. The larger the value, the higher the separation difficulty and the longer the mass transfer zone. It is obtained by fitting and determining through dynamic breakthrough experiments. Based on the complete breakthrough curve, the mass transfer driving force is calculated by interval integration (from breakthrough concentration threshold to saturation concentration). For low-concentration symmetrical breakthrough systems, it can be solved directly by analytical formulas. The average value is taken after multiple parallel experiments.

[0072] Step S303: Based on the preset minimum allowable penetration time, constrain the actual penetration time variable of impurities to determine the allowable non-uniformity coefficient of impurities.

[0073] The minimum allowable breakthrough time is the shortest adsorption cycle required by the adsorber and is the constraint boundary for breakthrough safety. The specific value is determined by the operator based on the actual adsorption situation of the adsorber.

[0074] The impurity non-uniformity coefficient is the maximum value of the air distribution non-uniformity coefficient corresponding to the condition where the actual penetration time of the impurity exactly equals the minimum allowable penetration time under the current airflow conditions. If this value is exceeded, the penetration time of the impurity will be lower than the constraint time, resulting in premature penetration. After determining the actual penetration time variable of the impurity, the time constraint equation is determined using the minimum allowable penetration time as the result of the actual penetration time variable of the impurity. This equation only contains the impurity non-uniformity coefficient variable. Given an unknown variable, the equation is solved using Newton's iterative method. An initial value of 1.2 is used as the initial value for the iteration. After substituting this value into the equation, the deviation between the penetration time and the constraint value is calculated. The non-uniformity coefficient is gradually corrected, and the maximum positive real root is determined when the relative deviation is less than 0.1%, which is then taken as the allowable non-uniformity coefficient variable for impurities. The value of is the allowable non-uniformity coefficient of impurities.

[0075] Step S304: Sort the allowable unevenness coefficients of impurities to determine the unevenness coefficient of air distribution.

[0076] In this step, the gas distribution non-uniformity coefficient is the same as that in step S102. The processing terminal sorts the allowable non-uniformity coefficients of all impurities and selects the smallest coefficient as the gas distribution non-uniformity coefficient to ensure that all components meet the breakthrough time constraint.

[0077] Reference Figure 4 The steps for determining the equilibrium adsorption capacity of a component based on its type and concentration include: Step S400: Obtain real-time intake temperature and component saturation adsorption capacity based on intake component type.

[0078] The real-time intake temperature is the thermodynamic temperature of the airflow, which is obtained by measuring the temperature with a thermometer and converting the Celsius temperature into the thermodynamic temperature.

[0079] The saturated adsorption capacity of a component is the maximum amount of adsorption when the surface of the adsorbent is completely covered by a monolayer. The larger the saturated adsorption capacity of a component, the higher the adsorption capacity of the adsorbent for that component. The saturated adsorption capacity of a component is determined by a static volumetric adsorption analyzer. Under constant temperature conditions, the partial pressure of impurities of the inlet component type is gradually increased, an adsorption isotherm is plotted, and the adsorption amount in the high plateau section is taken as the initial saturated adsorption capacity. The saturated adsorption capacity of the component is obtained by taking the average value after multiple measurements.

[0080] Step S401: Determine the Langmuir equilibrium constant of the intake components based on the intake component type and real-time intake temperature.

[0081] The component Langmuir equilibrium constant is the Langmuir equilibrium constant of the impurities corresponding to the inlet component type at the real-time inlet temperature, reflecting the strength of the adsorption force. The stronger the adsorption capacity, the larger the component Langmuir equilibrium constant. The Langmuir equilibrium constant of the impurities corresponding to the inlet component type at the reference temperature is obtained by correcting it using the van der Hoff equation. .

[0082] In the formula, Let Langmuir be the equilibrium constant of the component. For the first impurities, Let be the Langmuir equilibrium constant of the impurities at the reference temperature. For the first The heat of adsorption of certain impurities This is the universal gas constant. For real-time intake air temperature, This is a reference temperature.

[0083] The adsorption equilibrium constant changes with temperature according to the van der Hoff equation: Integral the equation from the reference temperature to the operating temperature: After integration and simplification, the above formula is obtained.

[0084] The Langmuir equilibrium constant of impurities at the reference temperature and the first The adsorption heat of the impurities was calibrated using a static capacity adsorption experiment. The specific process was as follows: An adsorption bed sample was prepared, and at least three experimental temperature points covering the actual operating temperature were selected. Adsorption isotherms were then tested at each temperature point. The sample temperature was adjusted to be near the temperature point, and after stabilization, the impurity gas was introduced into the sample. At least eight partial pressure gradients were set. After determining adsorption equilibrium, the equilibrium pressure and corresponding adsorption amount were recorded. For the equilibrium partial pressure-adsorption amount data at each temperature point, a nonlinear least squares fit was performed using the Langmuir isotherm as described in step S403 to obtain the saturated adsorption capacity and Langmuir equilibrium constant of the component at that temperature. The values ​​obtained from the fit at each temperature point were then used... Using the vertical axis as the ordinate, with Plot a curve on the x-axis, perform a linear fit on the data points, and the slope of the fitted line is... The slope determines the first The heat of adsorption of the impurities, with an intercept of Substituting 298.15K as the reference temperature into the fitted linear equation, we obtain the Langmuir equilibrium constant at the reference temperature.

[0085] Step S402: Determine the actual partial pressure of the components based on the mass concentration of the intake components.

[0086] The actual partial pressure of the component is the partial pressure of the impurities, and the specific calculation formula is as follows: .

[0087] In the formula, The actual partial pressure of the components, This refers to the mass concentration of the intake components. This is the universal gas constant. For real-time intake air temperature, For the first The molar mass of each impurity is obtained by the processing terminal from a database mapping impurities to their molar masses, based on the impurity type.

[0088] Ideal gas law Among them, the amount of substance , After substituting and rearranging, we obtain the above formula.

[0089] Step S403: Analyze the saturated adsorption capacity of the component, the Langmuir equilibrium constant of the component, and the actual partial pressure of the component to determine the equilibrium adsorption capacity of the component.

[0090] The component equilibrium adsorption capacity in this step is the same as that in step S300, and is calculated using the following formula: .

[0091] In the formula, For the first The component equilibrium adsorption capacity of the impurities, For the first The saturated adsorption capacity of the components of the impurity. , For the first impurities and the first The Langmuir equilibrium constant of the impurity components, , For the first impurities and the first The actual partial pressure of the components of the impurity.

[0092] Based on the single-component Langmuir model, the denominator incorporates the values ​​of all components. The term reflects the competitive occupation of adsorption sites by each component. The total number of adsorption sites is occupied by all impurities. The higher the partial pressure of a certain impurity, the larger the adsorption equilibrium constant and the higher the proportion of sites it occupies, while the lower the adsorption capacity of the other impurities.

[0093] Reference Figure 5The steps for determining the height of the component mass transfer unit based on the type of inlet gas component and the real-time empty tower gas velocity include: Step S500: Determine the maximum local gas velocity variable based on the real-time air tower gas velocity.

[0094] Among them, the maximum local gas velocity variable is the maximum local gas velocity in the adsorption bed cross section, which is obtained by multiplying the gas distribution non-uniformity coefficient variable and the real-time gas velocity in the adsorption bed. The gas distribution non-uniformity coefficient variable is an unknown quantity.

[0095] Step S501: Determine the component type correction factor based on the intake component type.

[0096] The component type correction coefficient is a coefficient used to correct for the differences in diffusion characteristics of different impurity molecules. Different impurity molecules have different sizes and polarities, resulting in significant differences in their diffusion capacity within the adsorption bed. The larger the molecule, the higher the diffusion barrier, the greater the mass transfer resistance, and the larger the correction coefficient. It is obtained by the treatment terminal through experimental calibration based on the impurities corresponding to the inlet component type. The specific process is as follows: a general adsorption bed is used, and the temperature, pressure, gas velocity, and concentration are all known reference values. After the gas is introduced, the impurity concentration at the outlet of the adsorption bed is monitored, and a complete breakthrough curve is recorded. Then, other impurities are replaced, and the breakthrough curves of all impurities are measured separately. The corresponding mass transfer unit height is calculated for each breakthrough curve. The mass transfer unit height of the reference component is used as the denominator, and the mass transfer unit height of the other impurities is used as the numerator. The ratio is the component type correction coefficient for that component.

[0097] Step S502: Obtain the aging correction coefficient of the adsorbent.

[0098] The adsorbent aging correction coefficient is a coefficient that corrects for the performance degradation of the adsorption bed after long-term use. The coefficient is not less than 1. During the long-term use of the adsorption bed, the adsorbent gradually pulverizes, and the micropores become blocked, which leads to an increase in mass transfer resistance and an increase in the height of the mass transfer unit. The more severe the aging, the larger the adsorbent aging correction coefficient. It is obtained through experimental calibration. The specific process is as follows: set the aging correction coefficient of the new adsorption bed to 1. After each adsorption cycle of the adsorption bed, measure and calculate the current height of the mass transfer unit. Use the reference mass transfer unit height as the denominator and the current mass transfer unit height as the numerator. The calculated ratio is the current aging correction coefficient.

[0099] Step S503: Analyze the component type correction coefficient, adsorbent aging correction coefficient, maximum local gas velocity variable, and preset baseline mass transfer characteristic coefficient to determine the height of the component mass transfer unit.

[0100] The reference mass transfer characteristic coefficient is the height of the mass transfer unit at a power of unit gas velocity. It is used to eliminate the confusion of parameter values ​​caused by the unclear gas velocity reference. It is obtained by calculating the ratio of the height of the mass transfer unit at the reference gas velocity to the power of the reference gas velocity.

[0101] The height of the component mass transfer unit in this step is the same as the height of the component mass transfer unit in step S301, and is calculated using the following formula: .

[0102] In the formula, For the height of the component mass transfer unit, This is a component type correction factor. This is the aging correction factor for the adsorbent. The reference mass transfer characteristic coefficient is used. For the maximum local air velocity variable, This is the preset air velocity influence index.

[0103] The adsorption process in an adsorption bed is typically controlled by external diffusion, with a gas-phase mass transfer coefficient of [missing information]. Real-time air tower velocity It is proportional to the power of 0.8, that is The mass transfer unit is highly Therefore, we can obtain: Therefore, the air speed influence index The value is 0.2. The above formula is obtained by combining the component type correction factor, the adsorbent aging correction factor, and the baseline mass transfer characteristic coefficient.

[0104] Reference Figure 6 The steps for analyzing the total pressure drop and gas distribution non-uniformity coefficient of the adsorption bed to determine the optimal total flow area include: Step S600: Constrain the total pressure drop of the adsorption bed based on the gas distribution non-uniformity coefficient to determine the minimum uniform pressure drop.

[0105] The minimum uniform pressure drop is the pressure drop of the uniformly distributed orifices that satisfies the constraint of the gas distribution non-uniformity coefficient. It is obtained by the treatment terminal constraining the total pressure drop of the adsorption bed based on the gas distribution non-uniformity coefficient. The specific method is described in [reference needed]. Figure 7 The steps.

[0106] Step S601: Obtain real-time airflow volumetric flow rate.

[0107] Among them, the real-time airflow volumetric flow rate is the real-time volumetric flow rate of the airflow, which is detected by the flow meter at the inlet of the air intake pipe.

[0108] Step S602: Analyze the real-time airflow volumetric flow rate and minimum average pressure drop to determine the optimal total flow area.

[0109] The optimal total flow area in this step is the same as the optimal total flow area in step S103, and is obtained by the processing terminal through analysis and calculation of the real-time airflow volumetric flow rate and the minimum average pressure drop. The specific method is described in [reference needed]. Figure 8 The steps.

[0110] Reference Figure 7 The steps for determining the minimum uniform pressure drop by constraining the total pressure drop of the adsorption bed based on the gas distribution non-uniformity coefficient include: Step S700: Analyze the air distribution non-uniformity coefficient and the preset air distribution structure coefficient to determine the uniform constraint coefficient.

[0111] The gas distribution structure coefficient is a quantitative value of the inherent homogenization ability of the equal distribution orifice. The smaller the coefficient, the more uniform the gas distribution of the equal distribution orifice under the same pressure drop. It is obtained through experimental calibration: using a common equal distribution orifice and adsorption bed, the gas velocity distribution is detected in the center, inner ring, middle ring and outer ring regions of the bed. The pressure drop of the equal distribution orifice is adjusted with multiple sets of known pressure drops, and the gas velocity at all measuring points under different pressure drops is recorded. The non-uniformity coefficient is calculated based on the quotient of the maximum gas velocity and the average gas velocity. At the same time, the bed pressure drop and the equal distribution pressure drop are determined. The square root of the quotient of the bed pressure drop and the equal distribution pressure drop is used as the abscissa, and the non-uniformity coefficient is used as the ordinate for linear fitting. The slope of the fitted straight line is the gas distribution structure coefficient.

[0112] The uniform constraint coefficient is the proportionality coefficient that converts the interlayer pressure drop into a uniformly distributed pressure drop, and it is calculated using the following formula: In the formula, The air distribution structure coefficient is... The gas distribution non-uniformity coefficient is derived from the empirical formula of the gas distribution non-uniformity coefficient and the pressure drop ratio.

[0113] Step S701: Calculate the product of the uniform constraint coefficient and the total pressure drop of the adsorption bed to generate the minimum uniform pressure drop.

[0114] The minimum average pressure drop in this step is consistent with the minimum average pressure drop in step S600, and is obtained by multiplying the uniform constraint coefficient and the total pressure drop of the adsorption bed by the processing terminal.

[0115] Reference Figure 8 The steps for determining the optimal total flow area by analyzing real-time airflow volumetric flow rate and minimum average pressure drop include: Step S800: Analyze the real-time intake density, minimum average pressure drop, and preset orifice flow coefficient to determine the flow area conversion ratio coefficient.

[0116] The orifice flow coefficient, used to correct for the contraction effect and viscous loss of the orifice, is the ratio of the actual flow rate to the theoretical flow rate. It affects the accuracy of the conversion between flow area and pressure drop. It was obtained through experimental calibration: using a common orifice, different flow rates were introduced, and the static pressure difference was measured. and actual volumetric flow rate The orifice flow rate formula is derived by modifying it. In the formula, The area of ​​the opening is... Calculate the orifice flow coefficient based on the airflow density. .

[0117] The flow-area conversion ratio factor is the ratio factor for converting volumetric flow rate into flow area, and it is calculated using the following formula: In the formula, For real-time intake air density, To minimize the average pressure drop, Let be the orifice flow coefficient. The flow rate formula for throttling through a thin-walled orifice is: The above formula is obtained after deformation.

[0118] Step S801: Calculate the product of the flow area conversion ratio coefficient and the real-time airflow volumetric flow rate to generate the optimal total flow area.

[0119] The optimal total flow area in this step is the same as the optimal total flow area in step S602, and is obtained by multiplying the flow area conversion ratio coefficient calculated by the processing terminal and the real-time airflow volumetric flow rate.

[0120] This application provides a computer-readable storage medium storing a computer program that can be loaded by a processor and executed to provide an adsorber efficiency optimization design method.

[0121] Computer storage media include, for example, USB flash drives, portable hard drives, read-only memory (ROM), random access memory (RAM), magnetic disks, optical disks, and other media that can store program code.

[0122] Based on the same inventive concept, embodiments of this application provide a smart terminal, including a memory and a processor, wherein the memory stores a computer program that can be loaded and executed by the processor to optimize the design method for the high efficiency of an adsorber.

[0123] Those skilled in the art will clearly understand that, for the sake of convenience and brevity, the above-described division of functional modules is used as an example. In practical applications, the above functions can be assigned to different functional modules as needed, that is, the internal structure of the device can be divided into different functional modules to complete all or part of the functions described above. The specific working process of the system, device, and unit described above can be referred to the corresponding process in the foregoing method embodiments, and will not be repeated here.

[0124] The above are all preferred embodiments of this application and are not intended to limit the scope of protection of this application. Any feature disclosed in this specification (including the abstract and drawings) may be replaced by other equivalent or similar features unless specifically stated otherwise. That is, unless specifically stated otherwise, each feature is only one example of a series of equivalent or similar features.

Claims

1. A method for optimizing the design of an adsorber to improve its efficiency, characterized in that, include: Obtain real-time intake gas density, real-time gas dynamic viscosity, real-time empty tower gas velocity, intake component type, and intake component mass concentration; The real-time inlet gas density, real-time gas dynamic viscosity, and real-time empty tower gas velocity were analyzed to determine the total pressure drop of the adsorption bed. The real-time empty tower gas velocity, inlet component type, and inlet component mass concentration were analyzed to determine the gas distribution non-uniformity coefficient. The total pressure drop and gas distribution non-uniformity coefficient of the adsorption bed were analyzed to determine the optimal total flow area. The optimal total flow area and the preset number of equal distribution holes are analyzed to determine the adjustment parameters for the equal distribution holes; Adjust the equal distribution holes of the airflow inlet pipe fitting according to the equal distribution hole adjustment parameters; The steps for analyzing real-time empty tower gas velocity, inlet component type, and inlet component mass concentration to determine the gas distribution non-uniformity coefficient include: The equilibrium adsorption capacity of the components is determined based on the type and mass concentration of the inlet components. The height of the component mass transfer unit is determined based on the type of inlet gas component and the real-time empty tower gas velocity. The component equilibrium adsorption capacity, component mass transfer unit height, real-time empty tower gas velocity, and inlet component mass concentration are substituted into the preset breakthrough time model to determine the actual breakthrough time variable of impurities. The actual penetration time variable of impurities is constrained and solved based on the preset minimum allowable penetration time in order to determine the allowable non-uniformity coefficient of impurities. The permissible non-uniformity coefficients of impurities are sorted to determine the air distribution non-uniformity coefficient.

2. The method for optimizing the high efficiency of an adsorber according to claim 1, characterized in that, The steps for analyzing real-time inlet gas density, real-time gas dynamic viscosity, and real-time empty tower gas velocity to determine the total pressure drop of the adsorption bed include: Obtain basic adsorption parameters; Based on a preset viscous resistance model, the basic adsorption parameters, real-time gas dynamic viscosity, and real-time empty tower gas velocity are calculated to generate real-time viscous resistance. Based on a preset inertial drag model, the basic adsorption parameters, real-time inlet gas density, and real-time empty tower gas velocity are calculated to generate real-time inertial drag. The sum of real-time viscous resistance and real-time inertial resistance is calculated to generate the total pressure drop of the adsorption bed.

3. The method for optimizing the high efficiency of an adsorber according to claim 1, characterized in that, The steps for determining the equilibrium adsorption capacity of a component based on the type and mass concentration of the inlet gas component include: Real-time intake temperature and saturated adsorption capacity of components are obtained based on the type of intake components. The Langmuir equilibrium constant of the components is determined based on the type of intake components and the real-time intake temperature. The actual partial pressure of the components is determined based on the mass concentration of the intake components. The saturated adsorption capacity, Langmuir equilibrium constant, and actual partial pressure of the components were analyzed to determine the equilibrium adsorption capacity of the components.

4. The method for optimizing the high efficiency of an adsorber according to claim 1, characterized in that, The steps for determining the height of the component mass transfer unit based on the inlet component type and real-time empty tower velocity include: Determine the maximum local gas velocity variable based on real-time tower gas velocity; Determine the component type correction factor based on the type of intake air components; Obtain the aging correction factor for the adsorbent; The component type correction coefficient, adsorbent aging correction coefficient, maximum local gas velocity variable, and preset baseline mass transfer characteristic coefficient are analyzed to determine the height of the component mass transfer unit.

5. The method for optimizing the high efficiency of an adsorber according to claim 1, characterized in that, The steps for analyzing the total pressure drop and gas distribution non-uniformity coefficient of the adsorption bed to determine the optimal total flow area include: The total pressure drop of the adsorption bed is constrained based on the gas distribution non-uniformity coefficient to determine the minimum uniform pressure drop; Obtain real-time airflow volumetric flow rate; The real-time airflow volumetric flow rate and minimum average pressure drop are analyzed to determine the optimal total flow area.

6. The method for optimizing the high efficiency of an adsorber according to claim 5, characterized in that, The steps for determining the minimum uniform pressure drop by constraining the total pressure drop of the adsorption bed based on the gas distribution non-uniformity coefficient include: The air distribution non-uniformity coefficient and the preset air distribution structure coefficient are analyzed to determine the uniformity constraint coefficient. Calculate the product of the uniform constraint coefficient and the total pressure drop of the adsorption bed to generate the minimum uniform pressure drop.

7. The method for optimizing the high efficiency of an adsorber according to claim 5, characterized in that, The steps for determining the optimal total flow area by analyzing real-time airflow volumetric flow rate and minimum average pressure drop include: The real-time intake density, minimum average pressure drop, and preset orifice flow coefficient are analyzed to determine the flow area conversion ratio coefficient. Calculate the product of the flow-area conversion ratio and the real-time airflow volumetric flow rate to generate the optimal total flow area.

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